CN111686645A - Micro-interface reinforced wax oil hydrogenation reaction system and method - Google Patents
Micro-interface reinforced wax oil hydrogenation reaction system and method Download PDFInfo
- Publication number
- CN111686645A CN111686645A CN201910196598.9A CN201910196598A CN111686645A CN 111686645 A CN111686645 A CN 111686645A CN 201910196598 A CN201910196598 A CN 201910196598A CN 111686645 A CN111686645 A CN 111686645A
- Authority
- CN
- China
- Prior art keywords
- gas
- micro
- wax oil
- hydrogen
- liquid
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 44
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 38
- 239000007788 liquid Substances 0.000 claims abstract description 173
- 239000000839 emulsion Substances 0.000 claims abstract description 96
- 238000006243 chemical reaction Methods 0.000 claims abstract description 91
- 238000000926 separation method Methods 0.000 claims abstract description 40
- 239000012071 phase Substances 0.000 claims abstract description 22
- 239000007791 liquid phase Substances 0.000 claims abstract description 20
- 238000012546 transfer Methods 0.000 claims abstract description 10
- 238000005728 strengthening Methods 0.000 claims abstract description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 121
- 239000007789 gas Substances 0.000 claims description 121
- 239000001257 hydrogen Substances 0.000 claims description 118
- 229910052739 hydrogen Inorganic materials 0.000 claims description 118
- 239000003054 catalyst Substances 0.000 claims description 74
- 239000002994 raw material Substances 0.000 claims description 37
- 239000000203 mixture Substances 0.000 claims description 36
- 229910052717 sulfur Inorganic materials 0.000 claims description 25
- 239000011593 sulfur Substances 0.000 claims description 25
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 24
- 150000002431 hydrogen Chemical class 0.000 claims description 13
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 11
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 11
- 230000005484 gravity Effects 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 5
- 230000008569 process Effects 0.000 abstract description 15
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 7
- 239000000463 material Substances 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 230000006835 compression Effects 0.000 abstract description 2
- 238000007906 compression Methods 0.000 abstract description 2
- 125000004122 cyclic group Chemical group 0.000 abstract description 2
- 230000016507 interphase Effects 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 177
- 238000004523 catalytic cracking Methods 0.000 description 15
- 239000000047 product Substances 0.000 description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 238000010586 diagram Methods 0.000 description 8
- 239000003502 gasoline Substances 0.000 description 8
- 239000002283 diesel fuel Substances 0.000 description 6
- 239000002002 slurry Substances 0.000 description 5
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 238000001514 detection method Methods 0.000 description 4
- 239000011344 liquid material Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000005086 pumping Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 3
- 238000004517 catalytic hydrocracking Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000007792 gaseous phase Substances 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- QVYYOKWPCQYKEY-UHFFFAOYSA-N [Fe].[Co] Chemical compound [Fe].[Co] QVYYOKWPCQYKEY-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 230000003111 delayed effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 2
- MOWMLACGTDMJRV-UHFFFAOYSA-N nickel tungsten Chemical group [Ni].[W] MOWMLACGTDMJRV-UHFFFAOYSA-N 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 239000002105 nanoparticle Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910052755 nonmetal Inorganic materials 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
Images
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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
-
- 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
-
- 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
- B01J8/001—Controlling catalytic processes
-
- 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
-
- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
-
- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
-
- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
- C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
-
- 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
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00823—Mixing elements
-
- 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
-
- 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
- C10G2300/70—Catalyst aspects
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (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 relates to a micro-interface reinforced wax oil hydrogenation reaction system and a method, comprising the following steps: the device comprises a liquid phase feeding unit, a gas phase feeding unit, a micro-interface generator, a fixed bed reactor and a separation tank. Compared with the traditional fixed bed reactor, the invention ensures that the gas is crushed to form micro bubbles with micron scale, and the micro bubbles are mixed with the wax oil to form emulsion, so as to increase the interphase area of gas phase and liquid phase, achieve the effect of strengthening mass transfer in a lower preset range, and reduce the pressure in the reaction process by 10-80 percent while ensuring the reaction efficiency; meanwhile, the mass transfer is greatly enhanced, so that the gas-liquid ratio can be greatly reduced, the material consumption of gas is reduced, and the energy consumption of subsequent gas cyclic compression is reduced; the method has the advantages of low process severity, high production safety, low ton product cost and strong market competitiveness.
Description
Technical Field
The invention relates to the technical field of wax oil processing, in particular to a micro-interface reinforced wax oil hydrogenation reaction system and a method.
Background
In recent years, with increasing shortage of petroleum resources, the trend of crude oil upgrading and degradation is getting worse, and with the development of economy, the demand for light oil products is increasing, so that maximum upgrading and benefit maximization of heavy oil become the pursuit targets of oil refining enterprises.
The main means for processing heavy oil are hydrocracking, catalytic cracking and delayed coking. Hydrocracking is difficult to process coker gas oil and residual oil due to large investment and high operation cost, so that the application of the hydrocracking is limited, and delayed coking is limited due to low liquid yield, poor product quality and other factors. The catalytic cracking has low operation cost, high yield of light oil products and good quality of wax oil products, and can process heavy inferior raw materials such as wax oil, residual oil and the like, thereby obtaining wide process application.
With the increasingly stricter quality standards of gasoline and diesel oil products in China, how to solve the problems of high sulfur content of catalytic cracking wax oil, high sulfur and aromatic hydrocarbon content of catalytic cracking diesel oil and low cetane number becomes a hotspot of research in recent years. At present, a plurality of catalytic cracking catalysts, auxiliary agents and process technologies are developed, wherein the catalytic cracking raw material pre-hydrogenation technology becomes an effective means for solving the problem of high sulfur content of catalytic wax oil. The pre-hydrogenation of the catalytic cracking raw material not only reduces the contents of sulfur, nitrogen and aromatic hydrocarbon, but also is beneficial to improving the catalytic cracking conversion rate, increasing the catalytic cracking light yield, reducing the sulfur content of wax oil, and improving the cetane numbers of wax oil olefin and diesel oil.
Among various methods for converting straight-run wax oil into light-weight wax oil, the process of hydrogenating wax oil as a catalytic cracking raw material is a good process route. Most of sulfur and nitrogen impurities are removed from the wax oil after hydrotreating, part of aromatic hydrocarbon is saturated, the hydrogen content is increased, the conversion rate of catalytic cracking raw materials can be increased, the coke yield is reduced, the yield of catalytic cracking light oil is increased, a product with improved quality is obtained, the sulfur content of the obtained wax oil is low, and the cetane numbers of wax oil olefin and diesel oil are also improved; meanwhile, the wax oil hydrotreating can also produce a byproduct of low-sulfur diesel oil with the concentration of 15 percent, and the diesel-gasoline ratio of a refinery is improved. Therefore, the process of using wax oil hydrotreating to generate oil as catalytic cracking raw material is also widely applied.
The coker gas oil has high sulfur and nitrogen contents, particularly high basic nitrogen contents, high carbon residue and high aromatic hydrocarbon contents, and is easy to lose catalytic activity when directly entering a catalytic cracking device for processing, so that the catalyst is seriously inactivated, the yield of the coker gas oil of the catalytic cracking device is low, and the yield of coke is increased, so that the coker gas oil is more necessary to be subjected to hydrogenation pretreatment compared with other coker gas oil components.
Chinese patent publication No.: CN104946299A discloses a wax oil circulating hydrogenation method, a design method and application thereof, wherein the hydrogenation method comprises the step of mixing wax oil produced by self of a slurry bed hydrogenation reactor with one or two of partial or all raw materials or catalysts to be hydrogenated to obtain raw material slurry with reduced viscosity, and the raw material slurry enters the slurry bed hydrogenation reactor for circulating hydrogenation. The wax oil used for the circulating hydrogenation accounts for 4-30wt% of the raw material to be hydrogenated, so that the kinematic viscosity of the raw material slurry is not higher than 750cSt at the temperature of not higher than 60 ℃.
It can be seen that the method has the following problems:
firstly, the hydrogen pressure used in the operation of the method is overlarge, so that potential safety hazards exist in the operation, a large amount of resources are consumed, and the process operation cost is high.
Secondly, the method needs higher reaction temperature to ensure the activity of the catalyst, and the energy consumption of the process is further increased while the reaction temperature is increased.
Third, the method mixes only hydrogen with the wax oil, so that hydrogen molecules cannot be sufficiently mixed with the wax oil, thereby causing a decrease in reaction efficiency.
Disclosure of Invention
Therefore, the invention provides a micro-interface reinforced wax oil hydrogenation reaction system and a micro-interface reinforced wax oil hydrogenation reaction method, which are used for solving the problem of overhigh energy consumption caused by the fact that hydrogen cannot be fully contacted with wax oil in the prior art.
In one aspect, the present invention provides a micro-interface enhanced wax oil hydrogenation reaction system, comprising:
the liquid-phase feeding unit is used for storing and conveying wax oil;
a gas phase feed unit to store and deliver hydrogen;
at least one Micro Interfacial Generator (MIG) which is respectively connected with the liquid phase feeding unit and the gas phase feeding unit, converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy of the bubbles to hydrogen bubbles, so that the hydrogen is crushed into Micro bubbles with the diameter of more than or equal to 1 mu m and less than 1mm to improve the mass transfer area between the wax oil and the hydrogen, and the wax oil and the Micro bubbles are mixed to form a gas-liquid emulsion after crushing, so that the reaction efficiency between the wax oil and the hydrogen is enhanced within a preset pressure range;
the fixed bed reactor is connected with the micro-interface generator and is used for loading the gas-liquid emulsion and providing a reaction space for wax oil and micro-bubbles in the gas-liquid emulsion;
and the separation tank is used for carrying out gas-liquid separation on the mixture of the treated wax oil and the mixed gas after the reaction in the fixed bed reactor.
Further, when the number of the micro-interface generators is more than or equal to two, the micro-interface generators are arranged in parallel and are arranged in series and/or in parallel, and the mixed gas-liquid emulsion is output to the fixed bed reactor to react.
Further, the micro-interface generator is one or more of a pneumatic micro-interface generator, a hydraulic micro-interface generator and an air-liquid linkage micro-interface generator.
Further, the liquid-phase feed unit comprises:
the liquid raw material tank is used for storing wax oil;
the feeding pump is connected with the liquid raw material tank and used for providing power for conveying the wax oil;
the liquid feeding preheater is connected with the feeding pump and used for preheating the wax oil conveyed by the feeding pump so as to enable the wax oil to reach a specified temperature, and a shunting pipeline is arranged at the outlet of the liquid feeding preheater and used for conveying the wax oil to the corresponding micro-interface generators respectively;
when the liquid-phase feeding unit is used for conveying the wax oil, the feeding pump starts to operate, the wax oil is pumped out of the liquid raw material tank and conveyed to the liquid feeding preheater, and the liquid feeding preheater heats the wax oil to a specified temperature and then conveys the wax oil to the micro-interface generator.
Further, the gas phase feed unit comprises:
a gas raw material buffer tank for storing hydrogen;
the compressor is connected with the gas raw material buffer tank and used for providing power for conveying hydrogen;
the gas feeding preheater is connected with the compressor and used for preheating the hydrogen conveyed by the compressor so as to enable the hydrogen to reach a specified temperature, and a shunting pipeline is arranged at the outlet of the gas feeding preheater and used for conveying the hydrogen to the corresponding micro-interface generators respectively;
when the gas-phase feeding unit is used for conveying hydrogen, the compressor starts to operate, the hydrogen is extracted from the gas raw material buffer tank and conveyed to the gas feeding preheater for preheating, and after preheating is completed, the gas feeding preheater conveys the hydrogen to the micro-interface generator so that the micro-interface generator can crush the hydrogen to a specified size.
Further, the fixed bed reactor comprises:
the reaction tank is a tank body and is used for providing a reaction space for the gas-liquid emulsion, and a discharge hole is formed in the reaction tank and is used for outputting the treated wax oil and the mixed gas after reaction;
and when the gas-liquid emulsion flows through the catalyst bed, the catalyst in the catalyst bed layer can contact with the gas-liquid emulsion to improve the reaction efficiency of all the substances in the gas-liquid emulsion.
Further, the knockout drum top is equipped with the gaseous phase export for carry gas mixture, and the knockout drum bottom is equipped with the liquid phase export, is used for carrying the wax oil after handling, works as after the reaction of the gas-liquid emulsion in the fixed bed reactor is accomplished, the knockout drum will react the mixture after the mixture transport to the knockout drum, the wax oil subsides to the knockout drum bottom and follow via the liquid phase export by the action of gravity in the mixture export in the system, gas mixture in the mixture follows via the gaseous phase export in the system.
In another aspect, the present invention provides a micro-interface enhanced wax oil hydrogenation reaction method, including:
step 1: adding a specified amount of wax oil to the liquid feed tank and a specified amount of hydrogen to the gaseous feed buffer tank before operating the system;
step 2: starting the system after the addition is finished, extracting wax oil from the liquid raw material tank through a feed pump, and extracting hydrogen from the gas raw material buffer tank through a compressor;
and step 3: enabling the wax oil to flow through a liquid feeding preheater, heating the wax oil to a specified temperature by the liquid feeding preheater, enabling hydrogen to flow through a gas feeding preheater, and heating the hydrogen to the specified temperature by the gas feeding preheater;
and 4, step 4: the wax oil is preheated and then shunted, the shunted wax oil is respectively conveyed to the corresponding micro-interface generators, the hydrogen is preheated and then shunted, and the shunted hydrogen is respectively conveyed to the corresponding micro-interface generators;
and 5: each micro-interface generator can control the ratio of the received wax oil to the hydrogen, break the hydrogen into micro-bubbles with a micron scale, and mix the micro-bubble wax oil with the micro-bubbles to form a gas-liquid emulsion after breaking;
step 6: after the micro-interface generators are mixed, outputting the gas-liquid emulsion to a fixed bed reactor, controlling the pressure and the temperature in the fixed bed reactor, and enabling the gas-liquid emulsion to flow in a specified direction;
and 7: allowing the gas-liquid emulsion to flow through the catalyst bed layer, controlling the airspeed of the gas-liquid emulsion, and enabling a catalyst arranged in the catalyst bed layer to promote the reaction of sulfur elements in the wax oil in the gas-liquid emulsion and the microbubbles to generate treated wax oil and hydrogen sulfide gas to treat the wax oil, wherein the hydrogen sulfide gas can form mixed gas with the hydrogen;
and 8: after the reaction is finished, the fixed bed reactor conveys a mixture formed by the treated wax oil and the mixed gas to the separation tank, the mixture is settled in the separation tank, the treated wax oil is settled on the lower layer of the separation tank and is output from the system through a liquid phase outlet for subsequent treatment, and the mixed gas stays on the upper layer of the separation tank after the treated wax oil is settled and is output from the system through a gas phase outlet for subsequent treatment.
Further, the reaction pressure in the fixed bed reactor in the step 6 is 1-14MPa, and the reaction temperature is 300-400 ℃.
Further, the space velocity of the gas-liquid emulsion in the step 7 is 0.5-1.5h-1。
Compared with the prior art, the invention has the beneficial effects that compared with the traditional fixed bed reactor, the invention ensures that the micro bubbles with micron scale are formed by crushing the gas, the micro bubbles and the wax oil are mixed to form gas-liquid emulsion, so as to increase the interphase area of gas-liquid two phases, achieve the effect of strengthening mass transfer in a lower preset range, and reduce the pressure in the reaction process by 10-80 percent while ensuring the reaction efficiency; meanwhile, the mass transfer is greatly enhanced, so that the gas-liquid ratio can be greatly reduced, the material consumption of gas is reduced, and the energy consumption of subsequent gas cyclic compression is reduced; the method has the advantages of low process severity, high production safety, low ton product cost and strong market competitiveness.
In particular, when different catalysts are used in the system of the present invention, the operation temperature can be properly adjusted according to the activity temperature of the catalyst, so the system of the present invention also has the advantages of greatly or doubly reducing the operation pressure and increasing the space velocity (handling capacity) under different catalyst systems.
In particular, micron-sized bubbles are not easy to coalesce in the process of collision with the movement of catalyst particles, and can basically keep the original form. Therefore, the contact area of gas and liquid in the fixed bed reactor is increased by geometric multiple, and the emulsification and mixing are more sufficient and stable, thereby achieving the effects of strengthening mass transfer and macroscopic reaction.
Further, a feeding pump and a compressor are respectively arranged in the liquid-phase feeding unit and the gas-phase feeding unit, so that when the system operates, the feeding pump and the compressor can respectively provide power for transportation of the wax oil and the hydrogen, the wax oil and the hydrogen can be conveyed to a specified device at a specified speed, and the operating efficiency of the system is improved.
Especially, still be equipped with liquid feeding preheater and gaseous feeding preheater respectively in liquid phase feed unit and the gaseous phase feed unit, when carrying wax oil and hydrogen, liquid feeding preheater and gaseous feeding preheater can preheat wax oil and hydrogen respectively, and like this, fixed bed reactor just need not to carry out high power heating to wax oil and hydrogen again when moving, has practiced thrift the resource consumption of fixed bed has reduced the energy consumption of system.
Further, the system is provided with at least one micro-interface generator, so that the system can enable wax oil and hydrogen to be fully mixed in different proportions by using a plurality of micro-interface generators, and the reaction efficiency of each substance in the gas-liquid emulsion can be remarkably improved when the system reacts with a catalyst.
In particular, at least one layer of catalyst bed plate is arranged in the fixed bed reactor, and the reaction rate of the gas-liquid emulsion can be further improved by fully contacting multiple layers of catalysts with the gas-liquid emulsion, so that the operation efficiency of the system is further improved.
Furthermore, the separating tank can separate the gas and the liquid of the mixture after reaction by using the gravity action, and no redundant separating device is needed to be used for the separating tank, so that the energy consumption of the system is further reduced.
In particular, the temperature and the pressure in the reaction tank are limited in the micro-interface enhanced wax oil hydrogenation reaction method, so that the energy consumption of the system is controlled to be minimum while the high-efficiency reaction of the gas-liquid emulsion in the reaction tank is ensured, and the energy consumption of the system can be further reduced.
Particularly, the air speed of the catalyst is controlled in the micro-interface enhanced wax oil hydrogenation reaction method, so that all substances in the gas-liquid emulsion can be reacted at the highest efficiency, and the operating efficiency of the system is further improved
Drawings
FIG. 1 is a schematic structural diagram of a bottom-mounted micro-interface enhanced wax oil hydrogenation reaction system according to the present invention;
FIG. 2 is a schematic structural diagram of a side-impact type micro-interface enhanced wax oil hydrogenation reaction system according to the present invention;
FIG. 3 is a schematic structural diagram of a bottom-mounted multi-stage micro-interface enhanced wax oil hydrogenation reaction system according to the present invention;
FIG. 4 is a schematic structural diagram of the overhead micro-interface enhanced wax oil hydrogenation reaction system according to the present invention.
Detailed Description
In order that the objects and advantages of the invention will be more clearly understood, the invention is further described below with reference to examples; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Preferred embodiments of the present invention are described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; 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 by those skilled in the art according to specific situations.
Embodiment of the System
Fig. 1 is a schematic structural diagram of a bottom-mounted Micro-interface enhanced wax oil hydrogenation reaction system according to an embodiment of the present invention, including a liquid feeding unit 1, a gas feeding unit 2, a Micro-interface generator 3 (MIG for short), a fixed bed reactor 4, and a separation tank 5; the micro-interface generator 3 is respectively connected with the liquid feeding unit 1 and the gas feeding unit 2 and is used for receiving the wax oil conveyed by the liquid feeding unit 1 and the hydrogen conveyed by the gas feeding unit 2; the fixed bed reactor 4 is connected with the micro-interface generator 3, and the output end of the micro-interface generator 3 is arranged in the fixed bed reactor 4 and used for outputting the gas-liquid emulsion in the micro-interface generator 3 to the fixed bed reactor; the separation tank 5 is connected with the fixed bed reactor 4 and used for receiving the mixture output by the fixed bed reactor 4 and carrying out gas-liquid separation on the mixture.
When the system is operated, the liquid feeding unit 1 is started, wax oil stored in the liquid feeding unit is conveyed to the micro-interface generator 3, meanwhile, the gas feeding unit 2 is started, hydrogen stored in the liquid feeding unit is conveyed to the micro-interface generator 3, the micro-interface generator 3 can smash the hydrogen, the hydrogen is smashed to a micrometer scale, micro bubbles with the diameter larger than or equal to 1 micrometer and smaller than 1mm are formed, after the smashing is completed, the micro-interface generator 3 mixes the micro bubbles with the wax oil to form a gas-liquid emulsion, the micro-interface generator 3 outputs the gas-liquid emulsion to the fixed bed reactor 4 after the mixing of the gas-liquid emulsion is completed, the gas-liquid emulsion is subjected to efficient reaction in the fixed bed reactor by controlling the temperature and the air pressure in the fixed bed reactor 4 and the airspeed of the gas-liquid emulsion, and the generated mixture is output to the separation tank 5 by the fixed bed reactor 4 after the reaction is completed, the separation tank 5 separates the treated wax oil in the mixture from the mixed gas of hydrogen and hydrogen sulfide and carries out subsequent treatment respectively. It can be understood by those skilled in the art that the system of the present invention can be used not only for the hydrotreating of wax oil, but also for the hydrogenation of diesel oil, gasoline, lubricating oil or other kinds of oil products with small molecular weight, as long as the system can be used for the hydrogenation of oil products to enable the oil products to perform high-efficiency reaction and achieve the specified standard after the reaction. Of course, the system of the present invention can also be used in other multiphase reactions, such as multiphase fluid formed by micron-scale particles, such as by micro-interface, micro-nano interface, ultramicro interface, micro-bubble biochemical reactor or micro-bubble biological reactor, using micro-mixing, micro-fluidization, micro-bubble fermentation, micro-bubble bubbling, micro-bubble mass transfer, micro-bubble reaction, micro-bubble absorption, micro-bubble oxygenation, micro-bubble contact, etc. to form multiphase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsified flow, multi-phase micro-structured flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, gas-liquid-solid emulsified flow, gas-liquid-solid micro-structured flow, micro-bubble flow, micro-foam flow, micro-gas-nano emulsified flow, micro-dispersed flow, two micro-mixed flow, micro-turbulence, micro-bubble, Or multiphase fluid (micro interface fluid for short) formed by micro-nano-scale particles, thereby effectively increasing the phase boundary mass transfer area between the gas phase and/or the liquid phase and/or the solid phase in the reaction process.
With continued reference to fig. 1, a liquid feed unit 1 according to an embodiment of the present invention includes: a liquid feedstock tank 11, a feed pump 12 and a liquid feed preheater 13; wherein the feed pump 12 is connected to the liquid feedstock tank 11 for pumping out the wax oil in the liquid feedstock tank 11; the liquid feeding preheater 13 is arranged at the output end of the feeding pump 12, and the liquid feeding preheater 13 is connected with the micro-interface generator 3, so as to preheat the wax oil output by the feeding pump 12 and convey the wax oil to the micro-interface generator 3 after preheating. When the liquid feed unit 1 is in operation, the feed pump 12 pumps the wax oil stored in the liquid feedstock tank 11 and delivers it to the liquid feed preheater 13, and the liquid feed preheater 13 preheats the wax oil to a specified temperature and delivers it to the micro-interface generator 3.
Specifically, the liquid material tank 11 is a tank body for storing wax oil, and the liquid material tank 11 is connected to the feed pump 12 for delivering the wax oil to a designated position through the feed pump 12 when the system is in operation. It is to be understood that the liquid material tank 11 may be a metal oil tank or a nonmetal oil tank as long as the liquid material tank 11 can be loaded with a predetermined amount of wax oil.
Specifically, the feed pump 12 is a centrifugal pump, which is disposed at the outlet of the liquid feedstock tank 11 to provide power for the transportation of the wax oil. When the liquid feed unit 1 is in operation, the feed pump 12 starts to operate, and the wax oil in the liquid feedstock tank 1 is pumped out and conveyed to the liquid feed preheating unit 13. It is understood that the type and power of the feed pump 12 are not particularly limited in this embodiment, as long as the feed pump 12 is capable of delivering wax oil at a given flow rate.
Specifically, the liquid feed preheater 13 is a preheater for preheating the wax oil, and a flow dividing pipe is disposed at an outlet of the liquid feed preheater 13 for respectively conveying the preheated wax oil to the interior of each of the micro-interface generators. When charge pump 12 carries wax oil, liquid feeding preheater 13 can be flowed through to wax oil, and liquid feeding preheater 13 can preheat wax oil and shunts after wax oil reaches the assigned temperature, carries wax oil to each micro-interface generator's inside respectively. It is understood that the kind of the preheater and the heating manner of the liquid feed preheater 13 are not particularly limited in this embodiment, as long as the liquid feed preheater 13 can preheat the wax oil to a specific temperature.
With continued reference to fig. 1, the gas feed unit 2 according to the embodiment of the present invention includes: a gas raw material buffer tank 21, a compressor 22, and a gas feed preheater 23; wherein, the compressor 22 is connected with the gas raw material buffer tank 21 and is used for pumping out the hydrogen in the gas raw material buffer tank 21; the gas feed preheater 23 is disposed at an output end of the compressor 22, and the gas feed preheater 23 is connected to the micro-interface generator 3, so as to preheat the hydrogen output by the compressor 22, and deliver the hydrogen to the micro-interface generator 3 after preheating. When the gas feed unit 2 is in operation, the compressor 22 extracts the hydrogen stored in the gas raw material buffer tank 21 and delivers the hydrogen to the gas feed preheater 23, and the gas feed preheater 23 delivers the hydrogen to the micro-interface generator 3 after preheating the hydrogen to a specified temperature.
Specifically, the gas material buffer tank 21 is a tank for storing hydrogen, and the gas material buffer tank 21 is connected to the compressor 22 for delivering hydrogen to a designated location through the compressor 22 when the system is in operation. It is to be understood that the present embodiment is not particularly limited as long as the gas raw material buffer tank 21 can load a prescribed amount of hydrogen gas.
Specifically, the compressor 22 is disposed at the outlet of the gas raw material buffer tank 21 to power the delivery of hydrogen gas. When the gas feed unit 2 is operated, the compressor 22 is operated to extract hydrogen gas from the gas raw material tank 2 and deliver the hydrogen gas to the gas feed preheating unit 23. It is to be understood that the power of the compressor 22 is not particularly limited in this embodiment, provided that the compressor 22 is capable of delivering hydrogen at a specified flow rate.
Specifically, the gas feed preheater 23 is a preheater for preheating hydrogen, and a flow dividing pipe is disposed at an outlet of the gas feed preheater 23 for respectively conveying the preheated hydrogen to the interior of each of the micro-interface generators. When the compressor 22 delivers hydrogen, the hydrogen will flow through the gas feed preheater 23, and the gas feed preheater 23 will preheat the hydrogen and split the hydrogen after the hydrogen reaches a predetermined temperature, delivering the hydrogen to the interior of each micro-interface generator. It is understood that the type of preheater and the heating method of the gas feed preheater 23 are not particularly limited in this embodiment, as long as the gas feed preheater 23 can preheat hydrogen to a predetermined temperature.
As shown in fig. 1, the micro-interface generator 3 of the present invention includes a first micro-interface generator 31 and a second micro-interface generator 32, the first micro-interface generator 31 and the second micro-interface generator 32 are vertically disposed at the bottom of the fixed bed reactor 4, the first micro-interface generator 31 and the second micro-interface generator 32 are parallel to each other, and each output port of the micro-interface generator is disposed inside the fixed bed reactor 4 to output the gas-liquid emulsion to the fixed bed reactor 4. When the micro-interface generator 3 operates, the first micro-interface generator 31 and the second micro-interface generator 32 can respectively receive wax oil and hydrogen with specified amounts, the first micro-interface generator 31 and the second micro-interface generator 32 can break the received hydrogen after the receiving is completed and break the hydrogen to a micron scale so as to form micro bubbles, the micro bubbles and the wax oil are mixed to form a gas-liquid emulsion after the breaking is completed, and the gas-liquid emulsion is output to the fixed bed reactor 4 after the mixing is completed. It can be understood that the connection mode of the micro-interface generator 3 and the fixed bed reactor 4 can be a pipeline connection, and the output end of the micro-interface generator 3 is arranged inside the fixed bed reactor 4 or in other connection modes, so long as the micro-interface generator 3 can output the gas-liquid emulsion to the inside of the fixed bed reactor 4.
Specifically, the first micro-interface generator 31 is an air-liquid linkage micro-interface generator, and is disposed at the bottom of the fixed bed reactor 4 and connected to the liquid feed preheater 13 and the gas feed preheater 23, respectively, so as to crush hydrogen and output an air-liquid emulsion formed by mixing micro-bubbles with wax oil to the inside of the fixed bed reactor 4. When the micro-interface generator 3 operates, the first micro-interface generator 31 receives the wax oil and the hydrogen gas in specified amounts, and crushes the hydrogen gas bubbles to a micron scale by using the pressure energy of the gas and the kinetic energy of the liquid, after the crushing is completed, the micro-bubbles and the wax oil are violently mixed to form a gas-liquid emulsion, and after the mixing is completed, the gas-liquid emulsion is output to the fixed bed reactor 4.
Specifically, the second micro-interface generator 32 is a pneumatic micro-interface generator, and is disposed at the bottom of the fixed bed reactor 4 and respectively connected to the liquid feed preheater 13 and the gas feed preheater 23, so as to crush hydrogen and output a gas-liquid emulsion formed by mixing micro-bubbles with wax oil to the inside of the fixed bed reactor 4. When the micro-interface generator 3 operates, the first micro-interface generator 31 receives the wax oil and the hydrogen gas in the specified amounts, and uses the pressure of the gas to crush the hydrogen gas bubbles to the micron scale, after the crushing, the micro-bubbles and the wax oil are violently mixed to form a gas-liquid emulsion, and after the mixing, the gas-liquid emulsion is output to the fixed bed reactor 4.
With continued reference to FIG. 1, the fixed bed reactor 4 of the present embodiment includes a reaction tank 41 and a catalyst bed 42; wherein the catalyst bed 42 is disposed inside the reaction tank 41 to load the catalyst. When the fixed bed reactor 4 operates, the micro-interface generator 3 can output the gas-liquid emulsion to the bottom of the reaction tank 41, the gas-liquid emulsion can gradually flow upwards after entering the bottom of the reaction tank 41, the gas-liquid emulsion is contacted with the catalyst arranged in the catalyst bed layer 42 in the flowing process and starts to react, so that sulfur elements contained in the wax oil in the gas-liquid emulsion react with the micro-bubbles to generate hydrogen sulfide, and the desulfurization of the wax oil is completed. It is to be understood that the catalyst may be one or a mixture of more of a molybdenum-based catalyst, a cobalt-based catalyst, a tungsten-based catalyst, a nickel-based catalyst, and an iron-based catalyst, as long as the catalyst can improve the reaction efficiency of each substance in the gas-liquid emulsion. The present invention is applicable to the above mentioned catalyst systems and also applicable to other hydrogenation catalyst systems not mentioned, as long as the system of the present invention can be used with different catalysts, the operation temperature can be properly adjusted according to the activity temperature of the catalyst used, and the system can still greatly or doubly reduce the operation pressure and increase the space velocity (throughput) under different catalyst systems.
Specifically, the reaction tank 41 is a cylindrical metal tank, and has a feed inlet at the bottom thereof for receiving the gas-liquid emulsion output from the micro-interface generator 3, and a discharge outlet at the top thereof, the discharge outlet being connected to the separation tank 5 for outputting the mixture after the reaction to the separation tank 5 for gas-liquid separation. Fixed bed reactor 4 is when the operation, 41 feed inlets of retort can be received the gas-liquid emulsion of 3 outputs at the micro-interface to for the gas-liquid emulsion provides reaction space, form the mixture of processing back wax oil and mist after the gas-liquid emulsion reaction is accomplished, retort 41 can be through the discharge gate with the mixture output extremely knockout drum 5. It is understood that the size and material of the reaction tank 41 are not particularly limited in this embodiment, as long as the reaction tank 41 can be loaded with a specified amount of gas-liquid emulsion and has a specified strength to withstand a preset reaction temperature and reaction pressure.
Specifically, the catalyst bed 42 is at least one bed plate, and a catalyst is fixedly disposed in the bed plate to increase the reaction speed of the gas-liquid emulsion. When the fixed bed reactor 4 operates, the gas-liquid emulsion in the reaction tank 41 flows upwards from the bottom of the reaction tank 41 and passes through the catalyst bed layer 42 in the flowing process, at this time, the catalyst in the catalyst bed layer 42 contacts with the gas-liquid emulsion, and the catalyst promotes the sulfur element in the wax oil in the gas-liquid emulsion to react with the micro bubbles to generate hydrogen sulfide so as to treat the wax oil. It is understood that the catalyst bed 42 may be a grid, mesh, ceramic ball or other type of structure, so long as the catalyst bed 42 is capable of securely holding the catalyst. Of course, the number of layers of the catalyst bed 42 may be one, two or other number of layers, as long as the catalyst bed 42 can achieve the specified reaction efficiency of each substance in the gas-liquid emulsion.
Referring to fig. 1, the separation tank 5 according to the embodiment of the present invention is a metal tank body, and is connected to the discharge port of the reaction tank 41 for performing gas-liquid separation on the mixture output from the reaction tank 41. And a gas phase outlet is formed in the top end of the separation tank 5 and used for outputting hydrogen and hydrogen sulfide gas, and a liquid phase outlet is formed in the bottom end of the separation tank and used for outputting the treated wax oil. After the fixed bed reactor 4 outputs the reacted mixture to the separation tank 5, the separation tank 5 performs gas-liquid separation on the mixed gas in the mixture and the treated wax oil by using the action of gravity, outputs the mixed gas containing hydrogen and hydrogen sulfide gas through a gas phase outlet, and outputs the treated wax oil through a liquid phase outlet. It is understood that the size and material of the separation tank 5 are not particularly limited in this embodiment, as long as the separation tank 5 has a predetermined strength and can hold a predetermined volume of the mixture.
Second embodiment of the System
Fig. 2 is a schematic structural diagram of a side-impact type micro-interface enhanced wax oil hydrogenation system according to an embodiment of the present invention, which uses the same components as those in the first embodiment of the system.
Different from the first embodiment of the system, in the present embodiment, a third micro-interface generator 33 is further disposed in the micro-interface generator 3, the third micro-interface generator 33 is disposed at the outlet of the gas feed preheater 23, and the third micro-interface generator 33 is connected in parallel with the second micro-interface generator 32 for respectively breaking up the hydrogen gas with a specified amount; the third micro-interface generator 33 is also connected in series with the first micro-interface generator 31 for performing multi-stage fragmentation of the hydrogen gas, thereby further reducing the diameter of the micro-bubbles.
First micro-interface generator 31 and second micro-interface generator 32 set up respectively on the lateral wall of retort 4 bottom, just first micro-interface generator 31 and second micro-interface generator 32 opposite direction set up for make first micro-interface generator 31 and second micro-interface generator 32 strike each other when exporting the gas-liquid emulsion, so that the gas-liquid emulsion mixes more evenly.
When the liquid feeding unit 1 and the gas feeding unit 2 respectively convey wax oil and hydrogen to the micro-interface generator, the third micro-interface generator 33 and the second micro-interface generator 32 respectively receive wax oil and hydrogen in specified amounts, the hydrogen is crushed to a micro-scale to form micro-bubbles and the wax oil and the micro-bubbles are mixed to form a gas-liquid emulsion, after the crushing, the third micro-interface generator 33 conveys the gas-liquid emulsion to the first micro-interface generator 31 to be further crushed, after the crushing is completed, the first micro-interface generator 31 and the second micro-interface generator 32 respectively output the gas-liquid emulsion inside to the bottom of the reaction tank 4 and move from bottom to top, because of the opposite arrangement of the two micro-interface generators, when the second micro-interface generator 32 and the third micro-interface generator 33 output the gas-liquid emulsion, the two gas-liquid emulsion streams can be flushed at the bottom of the reaction tank 41, thereby achieving the secondary mixing of the gas-liquid emulsion and further improving the mass transfer area of the wax oil and the micro bubbles between the gas-liquid emulsion.
Embodiment three of the System
Please refer to fig. 3, which is a schematic structural diagram of the bottom-mounted multi-stage micro-interface enhanced wax oil hydrogenation system according to the present invention, and the components of the system are the same as those of the first embodiment of the system.
Different from the first embodiment of the system, in the present embodiment, a plurality of catalyst beds 42 are disposed inside the reaction tank 41, and a gas inlet is disposed at the bottom of each catalyst bed 42 except for the lowermost catalyst bed 42, so as to deliver the hydrogen output by the gas feeding unit 2 to the inside of the reaction tank; a plurality of shunt tubes are arranged at the outlet of the gas feed preheating unit 23, and are used for conveying the preheated hydrogen to the gas inlet at the bottom of each catalyst bed layer 42, so as to ensure the hydrogen content in the reaction tank 41.
After the gas feeding preheating unit 23 finishes preheating the hydrogen, the hydrogen is output, a flow dividing pipe is arranged at an outlet of the gas feeding preheating unit, the hydrogen starts to be divided after being output and is respectively conveyed to corresponding parts, and a part of the hydrogen is conveyed into the micro-interface generator 3 and is smashed into micro-bubbles and forms a gas-liquid emulsion with the wax oil; another part of the hydrogen gas is delivered to the inside of the reaction tank 41 and is delivered to the bottom of each catalyst bed 42 through each of the gas inlets, respectively, so as to ensure the reaction efficiency of each substance in the gas emulsion in the reaction tank 41 by maintaining the hydrogen gas content inside the reaction tank 41 within a specified range.
Example four System
Fig. 4 is a schematic structural diagram of a top-mounted micro-interface enhanced wax oil hydrogenation system according to an embodiment of the present invention, which uses the same components as those in the first embodiment of the system.
Different from the above system embodiment, in this embodiment the micro interface generator 3 is arranged at the top of the reaction tank 41, and the discharge port of the reaction tank 41 is arranged at the bottom of the tank body, so that the gas-liquid emulsion output by the micro interface generator 3 flows from top to bottom in the reaction tank 41 through gravity, thereby reducing the energy consumption of the system.
When the first micro-interface generator 31 and the second micro-interface generator 32 output the gas-liquid emulsion to the reaction tank 41, the gas-liquid emulsion is located above the inside of the reaction tank 41 and moves downward under the action of gravity, contacts with the catalyst in the catalyst bed 42 during the movement of the gas-liquid emulsion and starts to react, and is output to the separation tank 5 through the discharge port at the bottom of the reaction tank 41 after the reaction is completed. Since the gas-liquid emulsion is moved downward by using the gravity, the system of the present embodiment does not need to provide power for the movement of the gas-liquid emulsion in the reaction tank 41, thereby further reducing the energy consumption required for the system.
Experimental example 1
The specific method and effect of the system of the present invention will be further described with reference to fig. 1.
A micro-interface reinforced wax oil hydrogenation reaction method comprises the following steps:
step 1: adding a prescribed amount of wax oil to the liquid feedstock tank 11 and a prescribed amount of hydrogen gas to the gas feedstock buffer tank 21 before operating the system;
step 2: starting the system after the addition is completed, pumping wax oil from the liquid feed tank 11 through the feed pump 12, and pumping hydrogen from the gas feed buffer tank 21 through the compressor 22;
and step 3: the wax oil flows through a liquid feed preheater 13, the liquid feed preheater 13 heats the wax oil to a specified temperature, the hydrogen flows through a gas feed preheater 23, and the gas feed preheater 23 heats the hydrogen to a specified temperature;
and 4, step 4: the wax oil is preheated and then shunted, the shunted wax oil is respectively conveyed to the corresponding micro-interface generators, the hydrogen is preheated and then shunted, and the shunted hydrogen is respectively conveyed to the corresponding micro-interface generators;
and 5: each micro-interface generator can control the ratio of the received wax oil to the hydrogen gas, smashes the hydrogen gas to a micron scale to form micro bubbles, and after the smashing is completed, each micro-interface generator can mix the micro bubbles and the wax oil to form a gas-liquid emulsion;
step 6: after the micro-interface generators are mixed, outputting the gas-liquid emulsion to a fixed bed reactor 4, controlling the pressure in the fixed bed reactor to be 1-14MPa and the temperature to be 300-400 ℃, and enabling the gas-liquid emulsion to flow in a specified direction;
and 7: the gas-liquid emulsion flows through the catalyst bed layer 42, and the space velocity of the gas-liquid emulsion is controlled to be 0.5-1.5h-1The catalyst arranged in the catalyst bed layer promotes the sulfur element in the wax oil in the gas-liquid emulsion to react with the micro bubbles to generate the treated wax oil and hydrogen sulfide gas to treat the wax oil, and the hydrogen sulfide gas can form mixed gas with the hydrogen;
and 8: after the reaction is finished, the fixed bed reactor conveys a mixture formed by the treated wax oil and the mixed gas to the separation tank 5, the mixture is settled in the separation tank 5, the treated wax oil is settled on the lower layer of the separation tank 5 and is output from the system through a liquid phase outlet for subsequent treatment, and the mixed gas stays on the upper layer of the separation tank 5 after the treated wax oil is settled and is output from the system through a gas phase outlet for subsequent treatment.
Specifically, in the step 5, the mixing ratio of the wax oil and the hydrogen in each micro-interface generator is as follows: the standard volume ratio of hydrogen to wax oil in the first micro-interface generator is 0.3: 1; the standard volume ratio of hydrogen to wax oil in the second micro-interface generator was 850: 1.
specifically, in the step 5, each micro-interface generator generates micro-bubbles with an average diameter of 1 μm or more and less than 1mm after breaking up the hydrogen gas.
The wax oil was hydrotreated using the above process and using the system of the first embodiment of the system, wherein:
in the step 6, the pressure inside the fixed reactor 4 is controlled at 4.3MPa, and the reaction temperature is controlled at 320 ℃.
The catalyst in the step 7 is FZC-302 type catalyst, and the space velocity of the gas-liquid emulsion is controlled to be 0.5h-1。
The wax oil before and after the system operation is detected respectively, and the detection results are as follows:
the sulfur content in the raw material wax oil before the system treatment is 110ppm, and the sulfur content in the treated wax oil after the system treatment is reduced to 40 ppm.
Experimental example two
The steps of the method in this example are the same as those in the first example.
Hydrodesulfurizing a wax oil using the above method and using the system of the first embodiment of the system, wherein:
in the step 5, the mixing ratio of the wax oil and the hydrogen in each micro-interface generator is as follows: the standard volume ratio of hydrogen to wax oil in the first micro-interface generator is 0.5: 1; the standard volume ratio of hydrogen to wax oil in the second micro-interface generator is 800: 1.
and in the step 5, each micro-interface generator generates micro-bubbles with the average diameter of more than or equal to 1 micrometer and less than 1mm after crushing the hydrogen.
In the step 6, the air pressure in the fixed reactor 4 is controlled at 6.2MPa, and the reaction temperature is controlled at 350 ℃.
The catalyst in the step 7 is iron-cobalt catalyst, and the space velocity of the gas-liquid emulsion is controlled to be 1.0h-1。
The wax oil before and after the system operation is detected respectively, and the detection results are as follows:
the sulfur content in the raw material gasoline before system treatment is 110ppm, and the sulfur content in the treated wax oil after system treatment is reduced to 45 ppm.
Experimental example III
The steps of the method in this example are the same as those in the first example.
Hydrodesulfurizing a wax oil using the above method and using the system of the first embodiment of the system, wherein:
in the step 5, the mixing ratio of the wax oil and the hydrogen in each micro-interface generator is as follows: the standard volume ratio of hydrogen to wax oil in the first micro-interface generator is 0.25: 1; the standard volume ratio of hydrogen to wax oil in the second micro-interface generator is 750: 1.
and in the step 5, each micro-interface generator generates micro-bubbles with the average diameter of more than or equal to 1 micrometer and less than 1mm after crushing the hydrogen.
In the step 6, the air pressure in the fixed reactor 4 is controlled at 8.7MPa, and the reaction temperature is controlled at 365 ℃.
The catalyst in the step 7 is a molybdenum-nickel catalyst, and the space velocity of the gas-liquid emulsion is controlled to be 1.3h-1。
The wax oil before and after the system operation is detected respectively, and the detection results are as follows:
the sulfur content in the raw material gasoline before system treatment is 110ppm, and the sulfur content in the treated wax oil after system treatment is reduced to 35 ppm.
Comparative example 1
In the first comparative example, a conventional fixed bed reactor system in the prior art is selected for hydrotreating wax oil, wherein:
the catalyst in the fixed bed reactor is a nickel-tungsten catalyst, the reaction temperature in the fixed bed reactor is 430 ℃, the hydrogen pressure is 20MPa, and the volume ratio of hydrogen to oil is 1100: 1, the space velocity of the mixture is 0.3h-1。
Gasoline before and after the system operation is detected respectively, and the detection results are as follows:
the sulfur content in the raw gasoline before the system treatment is 110ppm, and the sulfur content in the modified gasoline after the system treatment is reduced to 56 ppm.
The process parameters and the treated sulfur content in the three experimental examples and the comparative example are counted, and the statistical results are shown in table 1:
TABLE 1 comparison of data for wax oil treatment by each example system
| Catalyst and process for preparing same | Pressure of hydrogen | Reaction temperature | Airspeed | Gas to liquid ratio | Sulfur content after treatment | |
| Experimental example 1 | FZC-302 | 4.3MPa | 320℃ | 0.5h-1 | 850：1 | 40ppm |
| Experimental example two | Iron cobalt catalyst | 6.2MPa | 350℃ | 1.0h-1 | 800：1 | 45ppm |
| Experimental example III | Molybdenum-nickel catalyst | 8.7MPa | 365℃ | 1.3h-1 | 750：1 | 35ppm |
| Comparative example 1 | Nickel tungsten catalyst | 20MPa | 430℃ | 0.3h-1 | 1100：1 | 56ppm |
Therefore, the micro-interface reinforced wax oil hydrogenation reaction system and method can effectively remove sulfur in wax oil in the environments of medium and low pressure and low temperature.
So far, the technical solutions of the present invention have been described in connection with the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Equivalent changes or substitutions of related technical features can be made by those skilled in the art without departing from the principle of the invention, and the technical scheme after the changes or substitutions can fall into the protection scope of the invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and alterations to this invention will become apparent to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A micro-interface reinforced wax oil hydrogenation reaction system is characterized by comprising:
the liquid-phase feeding unit is used for storing and conveying wax oil;
a gas phase feed unit to store and deliver hydrogen;
at least one micro interface generator which is respectively connected with the liquid phase feeding unit and the gas phase feeding unit, converts the pressure energy of gas and/or the kinetic energy of liquid into the surface energy of bubbles and transmits the surface energy to hydrogen bubbles, so that the hydrogen is crushed into micro bubbles with the diameter of more than or equal to 1 mu m and less than 1mm to improve the mass transfer area between the wax oil and the hydrogen, and the wax oil and the micro bubbles are mixed to form a gas-liquid emulsion after being crushed so as to enhance the reaction efficiency between the wax oil and the hydrogen within a preset pressure range;
the fixed bed reactor is connected with the micro-interface generator and is used for loading the gas-liquid emulsion and providing a reaction space for wax oil and micro-bubbles in the gas-liquid emulsion;
and the separation tank is used for carrying out gas-liquid separation on the mixture of the treated wax oil and the mixed gas after the reaction in the fixed bed reactor.
2. The micro-interface enhanced wax oil hydrogenation reaction system according to claim 1, wherein when the number of the micro-interface generators is greater than or equal to two, each micro-interface generator is arranged in parallel and in series and/or in parallel, and is used for outputting the mixed gas-liquid emulsion to the fixed bed reactor for reaction.
3. The micro-interface enhanced wax oil hydrogenation reaction system of claim 2, wherein the micro-interface generator is one or more of a pneumatic micro-interface generator, a hydraulic micro-interface generator and a gas-liquid linkage micro-interface generator.
4. The micro-interface enhanced wax oil hydrogenation reaction system of claim 1, wherein the liquid-phase feeding unit comprises:
the liquid raw material tank is used for storing wax oil;
the feeding pump is connected with the liquid raw material tank and used for providing power for conveying the wax oil;
the liquid feeding preheater is connected with the feeding pump and used for preheating the wax oil conveyed by the feeding pump so as to enable the wax oil to reach a specified temperature, and a shunting pipeline is arranged at the outlet of the liquid feeding preheater and used for conveying the wax oil to the corresponding micro-interface generators respectively;
when the liquid-phase feeding unit is used for conveying the wax oil, the feeding pump starts to operate, the wax oil is pumped out of the liquid raw material tank and conveyed to the liquid feeding preheater, and the liquid feeding preheater heats the wax oil to a specified temperature and then conveys the wax oil to the micro-interface generator.
5. The micro-interface enhanced wax oil hydrogenation reaction system of claim 1, wherein the gas phase feed unit comprises:
a gas raw material buffer tank for storing hydrogen;
the compressor is connected with the gas raw material buffer tank and used for providing power for conveying hydrogen;
the gas feeding preheater is connected with the compressor and used for preheating the hydrogen conveyed by the compressor so as to enable the hydrogen to reach a specified temperature, and a shunting pipeline is arranged at the outlet of the gas feeding preheater and used for conveying the hydrogen to the corresponding micro-interface generators respectively;
when the gas-phase feeding unit is used for conveying hydrogen, the compressor starts to operate, the hydrogen is extracted from the gas raw material buffer tank and conveyed to the gas feeding preheater for preheating, and after preheating is completed, the gas feeding preheater conveys the hydrogen to the micro-interface generator so that the micro-interface generator can crush the hydrogen to a specified size.
6. The system of claim 1, wherein the fixed bed reactor comprises:
the reaction tank is a tank body and is used for providing a reaction space for the gas-liquid emulsion, and a discharge hole is formed in the reaction tank and is used for outputting the treated wax oil and the mixed gas after reaction;
and when the gas-liquid emulsion flows through the catalyst bed, the catalyst in the catalyst bed layer can contact with the gas-liquid emulsion to improve the reaction efficiency of all the substances in the gas-liquid emulsion.
7. The system of claim 1, wherein the top of the separation tank is provided with a gas outlet for delivering the mixture gas, the bottom of the separation tank is provided with a liquid outlet for delivering the treated wax oil, when the reaction of the gas-liquid emulsion in the fixed bed reactor is completed, the separation tank delivers the reacted mixture to the separation tank, the treated wax oil in the mixture settles to the bottom of the separation tank under the action of gravity and is output from the system through the liquid outlet, and the mixture gas in the mixture is output from the system through the gas outlet.
8. A micro-interface strengthening wax oil hydrogenation reaction method is characterized by comprising the following steps:
step 1: adding a specified amount of wax oil to the liquid feed tank and a specified amount of hydrogen to the gaseous feed buffer tank before operating the system;
step 2: starting the system after the addition is finished, extracting wax oil from the liquid raw material tank through a feed pump, and extracting hydrogen from the gas raw material buffer tank through a compressor;
and step 3: enabling the wax oil to flow through a liquid feeding preheater, heating the wax oil to a specified temperature by the liquid feeding preheater, enabling hydrogen to flow through a gas feeding preheater, and heating the hydrogen to the specified temperature by the gas feeding preheater;
and 4, step 4: the wax oil is preheated and then shunted, the shunted wax oil is respectively conveyed to the corresponding micro-interface generators, the hydrogen is preheated and then shunted, and the shunted hydrogen is respectively conveyed to the corresponding micro-interface generators;
and 5: each micro-interface generator can control the ratio of the received wax oil to the hydrogen, break the hydrogen into micro-bubbles with a micron scale, and mix the micro-bubble wax oil with the micro-bubbles to form a gas-liquid emulsion after breaking;
step 6: after the micro-interface generators are mixed, outputting the gas-liquid emulsion to a fixed bed reactor, controlling the pressure and the temperature in the fixed bed reactor, and enabling the gas-liquid emulsion to flow in a specified direction;
and 7: allowing the gas-liquid emulsion to flow through the catalyst bed layer, controlling the airspeed of the gas-liquid emulsion, and enabling a catalyst arranged in the catalyst bed layer to promote the reaction of sulfur elements in the wax oil in the gas-liquid emulsion and the microbubbles to generate treated wax oil and hydrogen sulfide gas to treat the wax oil, wherein the hydrogen sulfide gas can form mixed gas with the hydrogen;
and 8: after the reaction is finished, the fixed bed reactor conveys a mixture formed by the treated wax oil and the mixed gas to the separation tank, the mixture is settled in the separation tank, the treated wax oil is settled on the lower layer of the separation tank and is output from the system through a liquid phase outlet for subsequent treatment, and the mixed gas stays on the upper layer of the separation tank after the treated wax oil is settled and is output from the system through a gas phase outlet for subsequent treatment.
9. The method as claimed in claim 8, wherein the reaction pressure in the fixed bed reactor in step 6 is 1-14MPa, and the reaction temperature is 300-400 ℃.
10. The method of claim 8, wherein the space velocity of the gas-liquid emulsion in step 7 is 0.5-1.5h-1。
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910196598.9A CN111686645A (en) | 2019-03-15 | 2019-03-15 | Micro-interface reinforced wax oil hydrogenation reaction system and method |
| PCT/CN2019/090316 WO2020186641A1 (en) | 2019-03-15 | 2019-06-06 | Micro-interface enhanced wax oil hydrogenation reaction system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910196598.9A CN111686645A (en) | 2019-03-15 | 2019-03-15 | Micro-interface reinforced wax oil hydrogenation reaction system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111686645A true CN111686645A (en) | 2020-09-22 |
Family
ID=72475311
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910196598.9A Pending CN111686645A (en) | 2019-03-15 | 2019-03-15 | Micro-interface reinforced wax oil hydrogenation reaction system and method |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN111686645A (en) |
| WO (1) | WO2020186641A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112337409A (en) * | 2020-11-25 | 2021-02-09 | 重庆华峰化工有限公司 | Production system of hexamethylene diamine |
| CN114806636A (en) * | 2022-05-13 | 2022-07-29 | 中国海洋石油集团有限公司 | Hydrogen-oil efficient hydrogen-mixing reinforced wax oil hydrogenation system device and system method |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4347221A (en) * | 1980-03-13 | 1982-08-31 | Toyo Engineering Corporation | Catalytic converter |
| CN1640536A (en) * | 2004-01-12 | 2005-07-20 | 石油大学(北京) | Gas-liquid-solid composite reactor apparatus |
| CN101588864A (en) * | 2007-06-27 | 2009-11-25 | Hrd有限公司 | System and process for hydrodesulfurization, hydrodenitrogenation, or hydrofinishing |
| CN203229492U (en) * | 2013-04-03 | 2013-10-09 | 中国石油天然气股份有限公司 | Two-phase distillate oil hydrogenation reactor |
| CN103789005A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | Hydrogen dissolution method in two-phase hydrogenation reactor |
| CN105647577A (en) * | 2014-11-13 | 2016-06-08 | 中国石油天然气股份有限公司 | Hydrocarbon continuous liquid phase hydrogenation process method and device |
| CN105733662A (en) * | 2014-12-10 | 2016-07-06 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation reactor and process |
| CN106701179A (en) * | 2015-11-18 | 2017-05-24 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation device and method |
| CN107497372A (en) * | 2016-06-14 | 2017-12-22 | 中国石油天然气集团公司 | Hydrogenation reactor |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102311790B (en) * | 2010-07-07 | 2013-12-04 | 中国石油化工股份有限公司 | Liquid phase circular hydrogenation treatment method capable of improving mixed amount of hydrogen |
| CN104874315B (en) * | 2014-02-28 | 2017-11-24 | 中石化洛阳工程有限公司 | A kind of microbubble generator for strengthening hydrogenation technique |
| CN107335390B (en) * | 2017-08-30 | 2020-02-11 | 南京大学 | Modeling method for micro-interface enhanced reactor phase interface area structure effect regulation model |
| CN107474875B (en) * | 2017-09-22 | 2019-04-26 | 北京化工大学 | A kind of method of hypergravity oil and gasoline hydrofinishing |
-
2019
- 2019-03-15 CN CN201910196598.9A patent/CN111686645A/en active Pending
- 2019-06-06 WO PCT/CN2019/090316 patent/WO2020186641A1/en active Application Filing
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4347221A (en) * | 1980-03-13 | 1982-08-31 | Toyo Engineering Corporation | Catalytic converter |
| CN1640536A (en) * | 2004-01-12 | 2005-07-20 | 石油大学(北京) | Gas-liquid-solid composite reactor apparatus |
| CN101588864A (en) * | 2007-06-27 | 2009-11-25 | Hrd有限公司 | System and process for hydrodesulfurization, hydrodenitrogenation, or hydrofinishing |
| CN103789005A (en) * | 2012-11-03 | 2014-05-14 | 中国石油化工股份有限公司 | Hydrogen dissolution method in two-phase hydrogenation reactor |
| CN203229492U (en) * | 2013-04-03 | 2013-10-09 | 中国石油天然气股份有限公司 | Two-phase distillate oil hydrogenation reactor |
| CN105647577A (en) * | 2014-11-13 | 2016-06-08 | 中国石油天然气股份有限公司 | Hydrocarbon continuous liquid phase hydrogenation process method and device |
| CN105733662A (en) * | 2014-12-10 | 2016-07-06 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation reactor and process |
| CN106701179A (en) * | 2015-11-18 | 2017-05-24 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation device and method |
| CN107497372A (en) * | 2016-06-14 | 2017-12-22 | 中国石油天然气集团公司 | Hydrogenation reactor |
Non-Patent Citations (1)
| Title |
|---|
| 全国安全生产教育培训教材编审委员会 组织编写: "《加氢工艺作业》", 30 April 2013, 中国矿业大学出版社 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112337409A (en) * | 2020-11-25 | 2021-02-09 | 重庆华峰化工有限公司 | Production system of hexamethylene diamine |
| CN112337409B (en) * | 2020-11-25 | 2024-02-06 | 重庆华峰化工有限公司 | Production system of hexamethylenediamine |
| CN114806636A (en) * | 2022-05-13 | 2022-07-29 | 中国海洋石油集团有限公司 | Hydrogen-oil efficient hydrogen-mixing reinforced wax oil hydrogenation system device and system method |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2020186641A1 (en) | 2020-09-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN210079476U (en) | Hydrogenation reaction system of micro-interface enhanced fluidized bed | |
| CN111530380B (en) | Micro-interface enhanced reaction system and method for preparing ship fuel by heavy oil hydrogenation | |
| CN102049220B (en) | Method for enhancing gas-liquid mass transfer of ebullated bed hydrogenation reactor | |
| CN111359542A (en) | Micro-interface reinforced diesel hydrofining reaction system and method | |
| CN111482144A (en) | Bottom-mounted micro-interface enhanced reaction device and method for residual oil hydrogenation reaction | |
| CN111686653A (en) | Hydrogenation reaction system of micro-interface enhanced fluidized bed | |
| CN111686645A (en) | Micro-interface reinforced wax oil hydrogenation reaction system and method | |
| CN111686646A (en) | Gasoline hydrodesulfurization modification micro-interface enhanced reaction system and method | |
| CN108659882B (en) | Heavy oil hydrogenation method and hydrogenation system thereof | |
| CN111686647A (en) | Micro-interface reinforced lubricating oil hydrofining reaction system and method | |
| CN111686657A (en) | Oil-coal co-hydrogenation micro-interface enhanced fluidized bed reaction system | |
| CN210176791U (en) | Coal and biomass multistage liquefaction system | |
| CN210674823U (en) | Wash oil and direct liquefied coal oil mixed processing system | |
| CN112175667A (en) | Mixed oil hydrogenation micro-interface enhanced reaction system and method | |
| CN111686651A (en) | Micro-interface reinforced suspension bed hydrogenation reaction system and method | |
| CN111482145A (en) | Upper-mounted micro-interface enhanced reaction device and method for residual oil hydrogenation reaction | |
| CN112175665A (en) | Naphtha hydrogenation micro-interface enhanced reaction system and method | |
| AU2020102485A4 (en) | Micro-interface strengthening reaction system and method for preparing ship fuel by means of heavy oil hydrogenation | |
| CN111686652A (en) | Heavy oil hydrogenation micro-interface reinforced suspension bed reaction system and method | |
| CN112175664A (en) | Aviation kerosene hydrogenation micro-interface enhanced reaction system and method | |
| CN111686655A (en) | Coal tar hydrogenation micro-interface enhanced fluidized bed reaction system | |
| CN213506756U (en) | Preparation system of direct liquefaction of coal circulation solvent | |
| CN114437806B (en) | Heavy oil hydrotreating method | |
| CN110129089B (en) | Fluidized bed hydrogenation method | |
| CN112175649A (en) | Coal and biomass multistage liquefaction system and process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200922 |
|
| RJ01 | Rejection of invention patent application after publication |