CN112175650A - System and method for mixing and processing wash oil and direct coal liquefied oil - Google Patents
System and method for mixing and processing wash oil and direct coal liquefied oil Download PDFInfo
- Publication number
- CN112175650A CN112175650A CN201910600385.8A CN201910600385A CN112175650A CN 112175650 A CN112175650 A CN 112175650A CN 201910600385 A CN201910600385 A CN 201910600385A CN 112175650 A CN112175650 A CN 112175650A
- Authority
- CN
- China
- Prior art keywords
- oil
- hydrogen
- micro
- interface generator
- reaction
- 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
- 239000003245 coal Substances 0.000 title claims abstract description 86
- 238000012545 processing Methods 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000002156 mixing Methods 0.000 title claims description 31
- 239000001257 hydrogen Substances 0.000 claims abstract description 154
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 154
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 149
- 238000006243 chemical reaction Methods 0.000 claims abstract description 96
- 239000007788 liquid Substances 0.000 claims abstract description 71
- 239000002904 solvent Substances 0.000 claims abstract description 38
- 239000000203 mixture Substances 0.000 claims abstract description 34
- 238000005406 washing Methods 0.000 claims abstract description 26
- 239000000839 emulsion Substances 0.000 claims abstract description 24
- 238000012546 transfer Methods 0.000 claims abstract description 15
- 239000003921 oil Substances 0.000 claims description 244
- 238000000926 separation method Methods 0.000 claims description 30
- 238000003860 storage Methods 0.000 claims description 23
- 239000003054 catalyst Substances 0.000 claims description 18
- 239000010779 crude oil Substances 0.000 claims description 16
- 238000005984 hydrogenation reaction Methods 0.000 claims description 15
- 239000000126 substance Substances 0.000 claims description 11
- 239000000852 hydrogen donor Substances 0.000 claims description 9
- 230000003197 catalytic effect Effects 0.000 claims description 6
- 150000002431 hydrogen Chemical class 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 2
- 239000011369 resultant mixture Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 description 12
- 230000008569 process Effects 0.000 description 10
- 239000002994 raw material Substances 0.000 description 9
- 230000008901 benefit Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 238000005728 strengthening Methods 0.000 description 4
- 238000004945 emulsification Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 230000005501 phase interface Effects 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052755 nonmetal Inorganic materials 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 150000003254 radicals Chemical group 0.000 description 2
- 125000003118 aryl group Chemical group 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
- 230000000052 comparative effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- -1 hydrogen radicals Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
Images
Classifications
-
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- 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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
-
- 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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
-
- 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
- C10G7/00—Distillation of hydrocarbon oils
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- 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
Abstract
The invention provides a mixed processing system and a method for wash oil and direct coal liquefied oil, wherein the mixed processing system comprises the following steps: the system comprises a micro-interface generator, a reaction container, a feeding unit and a processing unit for reacting the obtained mixture; the micro-interface generator is connected with the feeding unit, the number of the micro-interface generator is more than or equal to 1, and the micro-interface generator is used for converting pressure energy of hydrogen and/or kinetic energy of mixed oil formed by washing oil and coal direct liquefaction oil into surface energy of hydrogen bubbles, so that the hydrogen bubbles are crushed into micron-sized bubbles with the diameter of 1 mu m or more and d less than 1mm, and the micron-sized bubbles and the mixed oil form gas-liquid emulsion, thereby increasing the mass transfer area between the hydrogen and the mixed oil, enabling the hydrogen and the mixed oil to fully react, and improving the hydrogen supply index of the obtained coal direct liquefaction hydrogen supply solvent.
Description
Technical Field
The invention relates to the technical field of mixed processing of wash oil and direct coal liquefied oil, in particular to a mixed processing system and method of wash oil and direct coal liquefied oil.
Background
At present, in the direct coal liquefaction process, the function of a solvent is very important, and the solvent can effectively reduce the occurrence of polymerization reaction, so that the yield of coal liquefied oil is improved. The solvent reduces the polymerization reaction by firstly dissolving and dispersing the free radical fragments generated by the reaction through the solubility of the solvent, and secondly, the solvent can also provide hydrogen radicals so that the free radical fragments become stable molecules in the reaction process. In the direct coal liquefaction process, the solvent is required to have good solubility for heavy aromatic substances and hydrogen donating properties. In the current direct coal liquefaction processes that achieve long-cycle continuous operation, the solvent comes from the direct coal liquefaction process itself and is recycled in the direct coal liquefaction process, also referred to as recycled solvent. At present, the hydrogen supply performance of the direct coal liquefaction hydrogen supply solvent becomes one of the key points in the research field of the direct coal liquefaction technology, and further improvement of the hydrogen supply index of the direct coal liquefaction hydrogen supply solvent or development of a solvent with excellent performance is an important aspect of the technical progress of the direct coal liquefaction.
Disclosure of Invention
In view of this, the invention provides a mixed processing system of wash oil and coal direct liquefied oil, aiming at enabling mixed oil formed by the wash oil and the coal direct liquefied oil to fully react with hydrogen and improving the hydrogen supply index of a coal direct liquefied hydrogen supply solvent generated by hydrogenation reaction.
In one aspect, the present invention provides a system for mixing and processing wash oil and coal direct liquefied oil, comprising: the system comprises a micro-interface generator, a reaction container, a feeding unit and a processing unit for reacting the obtained mixture; wherein the content of the first and second substances,
the micro-interface generator is connected with the feeding unit, the number of the micro-interface generator is more than or equal to 1, and the micro-interface generator is used for converting pressure energy of hydrogen and/or kinetic energy of mixed oil formed by washing oil and coal direct liquefaction oil into surface energy of hydrogen bubbles, so that the hydrogen bubbles are crushed into micron-sized bubbles with the diameter of 1 mu m or more and d less than 1mm, and the micron-sized bubbles and the mixed oil form gas-liquid emulsion, thereby increasing the mass transfer area between the hydrogen and the mixed oil, leading the hydrogen and the mixed oil to fully react, and improving the hydrogen supply index of the obtained coal direct liquefaction hydrogen supply solvent;
the reaction container is connected with the micro-interface generator and is used for providing a place for the reaction of the hydrogen and the mixed oil;
the feeding unit is used for conveying the hydrogen and the mixed oil into the micro-interface generator;
and the treatment unit of the mixture obtained by the reaction is connected with the reaction container and is used for treating the mixture obtained after the reaction in the reaction container is finished.
Further, in the mixed processing system of the washing oil and the direct coal-liquefied oil, the micro-interface generator is selected from one or more of a pneumatic micro-interface generator, a hydraulic micro-interface generator and a gas-liquid linkage micro-interface generator.
Further, in the mixed processing system of the washing oil and the direct coal liquefaction oil, when the number of the micro-interface generators is greater than or equal to two, the micro-interface generators are arranged in series and/or in parallel.
Further, in the above-mentioned washing oil and direct coal-to-liquid oil hybrid processing system, the feed unit includes: a hydrogen storage tank, an oil washing storage tank and a direct coal liquefaction oil storage tank; wherein the content of the first and second substances,
the hydrogen storage tank is connected with the micro-interface generator and is used for providing hydrogen;
the washing oil storage tank is connected with the micro-interface generator and is used for providing washing oil;
the coal direct liquefaction oil storage tank is connected with the micro-interface generator and is used for providing the coal direct liquefaction oil.
Further, in the above-mentioned washing oil and coal direct liquefaction oil mixing processing system, the processing unit of the mixture obtained by the reaction comprises: a separation tank, a rectifying tower and a product collecting tank; wherein the content of the first and second substances,
the separation tank is connected with the reaction container and is used for carrying out gas-liquid separation on the mixture, and after part of the separated hydrogen is discharged, the rest hydrogen is introduced into the micro-interface generator to provide hydrogen for the hydrogenation reaction of the mixed oil and the direct coal liquefaction oil;
the rectifying tower is connected with the separating tank and used for dividing the liquid separated by the separating tank into: light distillate, medium distillate and heavy distillate;
the product collecting tank is connected with the rectifying tower and is used for collecting products.
Further, in the above-mentioned washing oil and direct coal-to-liquid oil hybrid processing system, the product collection tank includes: a hydrogen donor solvent collection tank and a crude oil collection tank; wherein the content of the first and second substances,
the hydrogen donor solvent collection tank is connected with the rectifying tower and is used for collecting a hydrogen donor solvent consisting of the medium distillate oil and the heavy distillate oil;
the crude oil collecting tank is connected with the rectifying tower and is used for collecting crude oil formed by mixing the medium distillate oil and the light distillate oil.
Compared with the prior art, the invention has the advantages that compared with the traditional mixed processing system of the wash oil and the direct coal liquefaction oil, the micro-interface generator is arranged on the reaction container, the pressure energy and/or the kinetic energy of the liquid in the reaction process are converted into the surface energy of the hydrogen bubbles before the reaction raw materials enter the reactor for reaction, the hydrogen bubbles are crushed into micron-sized bubbles with the diameter of 1 mu m and d less than 1mm, the phase interface area between the mixed oil formed by the wash oil and the direct coal liquefaction oil and the hydrogen in the hydrogenation reaction process is effectively increased, the mass transfer efficiency between the mixed oil and the hydrogen is improved, the mixed oil and the hydrogen bubbles are mixed to form gas-liquid emulsion after crushing, the reaction efficiency between the mixed oil and the hydrogen is further strengthened in a lower pressure range, the gas-liquid ratio in the reaction process is effectively reduced, greatly reduces the material consumption of gas, and particularly improves the hydrogen supply index of the hydrogen supply solvent for direct coal liquefaction. In addition, the range of the preset operation condition can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, so that the full and effective reaction is further ensured, the reaction rate is further ensured, and the purpose of strengthening the reaction is achieved.
Particularly, in the mixed processing system of the wash oil and the direct coal liquefaction oil, the micro-interface generator can crush hydrogen bubbles into micron-sized bubbles, the micron-sized bubbles are not easy to coalesce during the motion collision with catalyst particles, the original form can be maintained, the contact area of gas and liquid in a reaction container is increased in geometric multiple, and the emulsification mixing is more sufficient and stable, so that the effects of mass transfer enhancement and macroscopic reaction are achieved.
Further, in the mixed processing system of wash oil and direct coal-liquid oil provided by the invention, the micro-interface generator can be selected from one or more of a pneumatic micro-interface generator, a hydraulic micro-interface generator and a gas-liquid linkage micro-interface generator, the selection of the type, the number and the arrangement mode of the micro-interface generator is carried out according to specific use requirements, and the hydrogen bubbles can be fully and effectively crushed into micron-sized bubbles before the mixed oil and hydrogen enter the reaction container, so that the hydrogen bubbles can be fully contacted with the mixed oil, and finally, the gas-liquid emulsion is formed, and the gas-liquid emulsion can be fully reacted under the catalytic action of the catalyst after entering the reaction container.
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.
On the other hand, the invention provides a mixed processing method of wash oil and coal direct liquefaction oil, which comprises the following steps:
(a) mixing a certain amount of washing oil and a certain amount of direct coal liquefaction oil, and introducing the mixture into a micro-interface generator;
(b) introducing a certain amount of hydrogen into the micro-interface generator, wherein the micro-interface generator converts pressure energy of the hydrogen and/or kinetic energy of mixed oil formed by washing oil and coal direct liquefaction oil into surface energy of hydrogen bubbles, so that the hydrogen bubbles are crushed into micron-sized bubbles, and the micron-sized bubbles and the mixed oil form a gas-liquid emulsion;
(c) introducing the gas-liquid emulsion into a reaction container, and fully reacting mixed oil contained in the gas-liquid emulsion with hydrogen under the catalytic action of a catalyst;
(d) introducing the mixture obtained after the reaction into a separation tank for gas-liquid separation, removing part of the separated hydrogen, introducing the rest hydrogen into a micro-interface generator to provide hydrogen for the hydrogenation reaction of the mixed oil and the direct coal liquefaction oil, and introducing the separated liquid into a rectifying tower;
(e) dividing the liquid in the rectifying tower into: the method comprises the steps of mixing light distillate oil, medium distillate oil and heavy distillate oil, introducing the mixture into a crude oil collection tank, and introducing the mixture of the medium distillate oil and the heavy distillate oil into a hydrogen supply solvent collection tank.
Further, in the method for mixing and processing the wash oil and the coal direct liquefaction oil, the volume ratio of the mixed oil to the hydrogen is 200-1000.
Further, in the method for mixing and processing the wash oil and the direct coal liquefaction oil, the reaction temperature in the step (c) is 320-400 ℃.
Further, in the method for mixing and processing the wash oil and the coal direct liquefaction oil, the reaction pressure in the step (c) is 2.0-10.0 MPa.
Compared with the prior art, the invention has the advantages that compared with the traditional mixed processing technology of the wash oil and the direct coal liquefaction oil, the invention has the advantages that the micro-interface generator is arranged on the reaction container, the pressure energy and/or the kinetic energy of the liquid in the reaction process are converted into the surface energy of the hydrogen bubbles before the reaction raw materials enter the reactor for reaction, the hydrogen bubbles are crushed into micron-sized bubbles with the diameter of 1 mu m and d of more than or equal to 1mm, the phase interface area between the mixed oil formed by the wash oil and the direct coal liquefaction oil and the hydrogen in the hydrogenation reaction process is effectively increased, the mass transfer efficiency between the mixed oil and the hydrogen is improved, the mixed oil and the hydrogen bubbles are mixed to form gas-liquid emulsion after crushing, the reaction efficiency between the mixed oil and the hydrogen is further strengthened in a lower pressure range, the gas-liquid ratio in the reaction process is effectively reduced, greatly reduces the material consumption of gas, and particularly improves the hydrogen supply index of the hydrogen supply solvent for direct coal liquefaction. In addition, the range of the preset operation condition can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, so that the full and effective reaction is further ensured, the reaction rate is further ensured, and the purpose of strengthening the reaction is achieved.
Particularly, in the mixed processing technology of the wash oil and the direct coal liquefaction oil, the micro-interface generator can crush hydrogen bubbles into micron-sized bubbles, the micron-sized bubbles are not easy to coalesce during the motion collision with catalyst particles, the original form can be maintained, the contact area of gas and liquid in a reaction container is increased in geometric multiple, and the emulsification and mixing are more sufficient and stable, so that the effects of mass transfer enhancement and macroscopic reaction are achieved.
Furthermore, the method disclosed by the invention is low in process severity, high in production safety and strong in market competitiveness.
Furthermore, in the method for the hydrogenation reaction of the micro-interface enhanced aviation kerosene, provided by the invention, the airspeed of the catalyst is also controlled, 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
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 refer to like parts throughout the drawings. In the drawings:
FIG. 1 is a schematic structural diagram of a system for mixing and processing wash oil and coal direct liquefaction oil according to an embodiment of the present invention.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
Referring to fig. 1, a system for mixing and processing wash oil and coal direct liquefaction oil according to an embodiment of the present invention includes: a micro-interface generator 4, a reaction vessel 5, a feeding unit, a processing unit of the mixture obtained by the reaction, and a conduit; the micro-interface generator 4 is connected with the feeding unit, the number of the micro-interface generator is more than or equal to 1, and the micro-interface generator is used for converting pressure energy of hydrogen and/or kinetic energy of mixed oil formed by washing oil and coal direct liquefaction oil into surface energy of hydrogen bubbles, so that the hydrogen bubbles are crushed into micron-sized bubbles, the micron-sized bubbles and the mixed oil form gas-liquid emulsion, the mass transfer area between the hydrogen and the mixed oil is increased, the hydrogen and the mixed oil are fully reacted, and the hydrogen supply index of the obtained coal direct liquefaction hydrogen supply solvent is improved; the reaction vessel 5 is connected with the micro-interface generator 4 and is used for providing a place for the reaction of the hydrogen and the mixed oil; the feeding unit is used for conveying the hydrogen and the mixed oil into the micro-interface generator 4; the treatment unit of the mixture obtained from the reaction is connected to the reaction vessel 5 for treating the mixture obtained after the reaction in the reaction vessel 5 is completed, and the conduits are connected between the respective parts for transporting gas and liquid.
It is understood that the type and number of the micro-interface generators 4 are not limited in this embodiment, and the micro-interface generators 4 are selected from one or more of a pneumatic micro-interface generator, a hydraulic micro-interface generator, and an air-liquid linkage micro-interface generator; particularly, when the number of the micro-interface generators 4 is greater than or equal to two, the micro-interface generators 4 are arranged in series and/or in parallel; meanwhile, the type of the catheter is not limited in the embodiment, and only the catheter can play a transportation role.
Specifically, the feed unit comprises: a hydrogen storage tank 1, an oil washing storage tank 2 and a coal direct liquefaction oil storage tank 3; wherein, the hydrogen storage tank 1 is a tank body which is connected with the micro-interface generator 4 and is used for providing hydrogen; the washing oil storage tank 2 is a tank body, is connected with the micro-interface generator 4 and is used for providing washing oil; the coal direct liquefaction oil storage tank 3 is a tank body, and is connected with the micro-interface generator 4 to provide the coal direct liquefaction oil. It should be understood that the type of each storage tank is not limited in this embodiment, and the storage tanks may be made of metal or nonmetal, and only need to be capable of bearing the formulated raw materials.
Specifically, the treatment unit of the reaction mixture includes: a separation tank 6, a rectifying tower 7 and a product collecting tank; the separation tank 6 is connected with the reaction vessel 5 and is used for carrying out gas-liquid separation on the mixture, and after a part of separated hydrogen is discharged, the rest hydrogen is introduced into the micro-interface generator 4 to provide hydrogen for the hydrogenation reaction of the mixed oil and the direct coal liquefaction oil; the rectifying tower 7 is connected with the separation tank 6 and used for dividing the liquid separated by the separation tank 6 into: light distillate, medium distillate and heavy distillate; the product collection tank is connected with the rectifying tower 7 and is used for collecting products.
Specifically, the separation tank 6 is provided with a gas outlet and a liquid outlet, and the hydrogen separated by the separation tank 6 is separated out through the gas outlet, wherein a part of the hydrogen is introduced into the micro-interface generator 4 to be used as a hydrogen raw material for the mixed oil hydrogenation reaction; the liquid separated by the separation tank 6 is introduced into the rectifying tower 7 through a liquid outlet; it is to be understood that the type of the separation tank 6 is not limited in this embodiment, and it may be a metal product or a non-metal product, and it is only necessary that the separation tank 6 can separate the gas and the liquid of the mixture.
Specifically, rectifying column 7 is equipped with three discharge gates, three the discharge gate is respectively: the device comprises a light distillate oil discharge port, a medium distillate oil discharge port and a heavy distillate oil discharge port, wherein the light distillate oil, the medium distillate oil and the heavy distillate oil are respectively separated through the light distillate oil discharge port, the medium distillate oil discharge port and the heavy distillate oil discharge port. Wherein, one part of the separated medium distillate oil is introduced into a conduit for separating the light distillate oil and is mixed with the light distillate oil to form crude oil, and the other part of the separated medium distillate oil is introduced into a conduit for heavy distillate oil and is mixed with the heavy distillate oil to form a hydrogen supply solvent.
Specifically, the product collection tank includes: a hydrogen donor solvent collection tank 8 and a crude oil collection tank 9; wherein, the hydrogen donor solvent collecting tank 8 is connected with the rectifying tower 7 and is used for collecting the hydrogen donor solvent consisting of the medium distillate oil and the heavy distillate oil; the crude oil collecting tank 9 is connected with the rectifying tower 7 and is used for collecting crude oil formed by mixing the medium distillate oil and the light distillate oil.
Referring to fig. 1, the working process of the mixed processing system of wash oil and coal direct liquefaction oil of this embodiment is as follows: hydrogen is conveyed to the micro-interface generator 4 from the hydrogen storage tank 1, wash oil is conveyed to the micro-interface generator 4 from the wash oil storage tank 2, coal direct liquefaction oil is conveyed to the micro-interface generator 4 from the coal direct liquefaction oil storage tank 3, the micro-interface generator 4 converts pressure energy of the hydrogen and/or kinetic energy of mixed oil formed by the wash oil and the coal direct liquefaction oil into surface energy of hydrogen bubbles, the hydrogen bubbles are broken into micron-sized bubbles with the diameter of 1 mu m or more and d less than 1mm, the micron-sized bubbles and the mixed oil form a gas-liquid emulsion, the gas-liquid emulsion enters the reaction container 5, the contained hydrogen and the mixed oil fully react under the catalytic action of a hydrogenation refined catalyst, a mixture obtained after the reaction is fed into the separation tank 6, and the separation tank 6 performs gas-liquid separation on the mixture, after the hydrogen of separation emits partly, the remaining part lets in conduct in the micro interface generator 4 as the hydrogen raw materials of miscella hydrogenation, the liquid of separation lets in the rectifying column 7, rectifying column 7 will liquid divide into light distillate oil, medium distillate oil and heavy distillate oil, wherein light distillate oil with medium distillate oil mixes and lets in the collection of crude oil is in order to carry out the collection of crude oil in the crude oil collection tank 9, medium distillate oil with heavy distillate oil mixes and lets in the collection of hydrogen supply solvent collection tank 8 in order to carry out the collection of hydrogen supply solvent.
Compared with the prior art, the invention has the advantages that compared with the traditional mixed processing system of the wash oil and the direct coal liquefaction oil, the micro-interface generator 4 is arranged on the reaction container 5, the pressure energy and/or the kinetic energy of the liquid in the reaction process are converted into the surface energy of the hydrogen bubbles before the reaction raw materials enter the reactor for reaction, the hydrogen bubbles are crushed into micron-sized bubbles with the diameter of 1 mu m and d less than 1mm, the phase interface area between the mixed oil formed by the wash oil and the direct coal liquefaction oil and the hydrogen in the hydrogenation reaction process is effectively increased, the mass transfer efficiency between the mixed oil and the hydrogen is improved, the thickness of a liquid film is reduced, the mass transfer resistance is reduced, the mixed oil and the micron-sized bubbles of the hydrogen are mixed to form a gas-liquid substance after crushing, and the reaction efficiency between the mixed oil and the hydrogen is further strengthened in a lower pressure range, the gas-liquid ratio in the reaction process is effectively reduced, the material consumption of gas is greatly reduced, and particularly, the hydrogen supply index of the hydrogen supply solvent for direct coal liquefaction is improved.
Particularly, in the mixed processing system of the wash oil and the direct coal liquefaction oil, the micro-interface generator 4 can crush hydrogen bubbles into micron-sized bubbles, the micron-sized bubbles are not easy to coalesce during the motion collision with catalyst particles, the original form can be maintained, the contact area of gas and liquid in the reaction container 5 is increased in geometric multiple, and the emulsification and mixing are more sufficient and stable, so that the effects of mass transfer enhancement and macroscopic reaction are achieved.
Further, in the mixed processing system of wash oil and direct coal-to-liquid oil provided by the invention, the micro-interface generator 4 may be selected from one or more of a pneumatic micro-interface generator 4, a hydraulic micro-interface generator 4 and a gas-liquid linkage micro-interface generator 4, and the selection of the type, number and arrangement mode of the micro-interface generator 4 is performed according to specific use requirements, so that the hydrogen bubbles can be fully and effectively crushed into micron-sized bubbles before the mixed oil and hydrogen enter the reaction container 5, so that the hydrogen bubbles can be fully contacted with the mixed oil, and a gas-liquid emulsion is formed, and finally, the gas-liquid emulsion can be fully reacted under the catalytic action of a catalyst after entering the reaction container 5.
Further, the separation tank 6 can separate the gas and the liquid of the mixture after reaction by using the gravity action, and no redundant separation device is needed to be used for the separation tank 6, so that the energy consumption of the system is further reduced.
It can be understood that the range of the preset operation conditions can be flexibly adjusted according to different raw material compositions, different product requirements or different catalysts, so as to ensure the full and effective reaction, further ensure the reaction rate and achieve the purpose of strengthening the reaction. Meanwhile, in the present embodiment, the kind of the catalyst is not particularly limited as long as the strengthening reaction can be smoothly performed.
The method and effect of the mixed processing system of wash oil and coal direct liquefaction oil of the present invention will be further described with reference to the following embodiments.
(a) Mixing a certain amount of washing oil and a certain amount of direct coal liquefaction oil, and introducing the mixture into a micro-interface generator 4;
(b) introducing a certain amount of hydrogen into the micro-interface generator 4 (the volume ratio of the hydrogen to the mixed oil is 200-1000), wherein the micro-interface generator 4 converts the pressure energy of the hydrogen and/or the kinetic energy of the mixed oil formed by the washing oil and the direct coal liquefaction oil into the surface energy of hydrogen bubbles, so that the hydrogen bubbles are crushed into micron-sized bubbles, and the micron-sized bubbles and the mixed oil form a gas-liquid emulsion;
(c) introducing the gas-liquid emulsion into a reaction container 5, and allowing the mixed oil contained in the gas-liquid emulsion and hydrogen to fully react under the catalytic action of a hydrogenation refined catalyst, wherein the reaction pressure is 2.0-10.0MPa, the reaction temperature is 320-400 ℃, and the volume space velocity is 1-2.5h-1。
(d) Introducing the mixture obtained after the reaction into a separation tank 6 for gas-liquid separation, discharging a part of the separated hydrogen, introducing the rest hydrogen into the micro-interface generator 4 again to provide hydrogen for the hydrogenation reaction of the mixed oil and the direct coal liquefaction oil, and introducing the separated liquid into a rectifying tower 7;
(e) the liquid in the rectifying column 7 is divided into: the method comprises the steps of mixing light distillate oil, medium distillate oil and heavy distillate oil, introducing the mixture into a crude oil collecting tank 9, and introducing the mixture of the medium distillate oil and the heavy distillate oil into a hydrogen supply solvent collecting tank 8.
Example 1
In this embodiment, the volume ratio of the hydrogen to the mixed oil in the micro-interface generator 4 is 1000: 1; the average diameter of the micron-sized bubbles is that d is more than or equal to 1 mu m and less than 1mm, the air pressure in the reaction container 5 is controlled at 10MPa, the reaction temperature is controlled at 400 ℃, and the volume is controlledThe volume space velocity is 2.5h-1The active component of the catalyst is oxide of cobalt and the carrier is AL2O3And detecting that the hydrogen supply index of the obtained coal direct liquefaction hydrogen supply solvent is 24.1 mg/g.
Example 2
In this embodiment, the volume ratio of the hydrogen to the mixed oil in the micro-interface generator 4 is 550: 1; the average diameter of the micron-sized bubbles is that d is more than or equal to 1 mu m and less than 1mm, the air pressure in the reaction vessel 5 is controlled at 5.5MPa, the reaction temperature is controlled at 350 ℃, and the volume space velocity is 2.0h-1The active component of the catalyst is Mo oxide and the carrier is AL2O3And detecting that the hydrogen supply index of the obtained coal direct liquefaction hydrogen supply solvent is 23.2 mg/g.
Example 3
In this embodiment, the volume ratio of the hydrogen to the mixed oil in the micro-interface generator 4 is 200: 1; the average diameter of the micron-sized bubbles is that d is more than or equal to 1 mu m and less than 1mm, the air pressure in the reaction vessel 5 is controlled at 2.0MPa, the reaction temperature is controlled at 320 ℃, and the volume space velocity is 1.0h-1The active component of the catalyst is oxide of Ni and the carrier is AL2O3And detecting that the hydrogen supply index of the obtained coal direct liquefaction hydrogen supply solvent is 22.3 mg/g.
Comparative example
In the embodiment, a conventional reaction system is selected for mixing and processing the wash oil and the coal direct liquefied oil, wherein the air pressure in the reaction vessel is controlled at 8.7MPa, the reaction temperature is controlled at 380 ℃, and the volume space velocity is 1.0h-1The active component of the catalyst is oxide of Ni and the carrier is AL2O3And detecting that the hydrogen supply index of the obtained coal direct liquefaction hydrogen supply solvent is 20.6 mg/g.
Obviously, the hydrogen is broken into micron-sized bubbles by the micro-interface generator, so that the micron-sized bubbles and the mixed oil form gas-liquid emulsion, the mass transfer area between the hydrogen and the mixed oil is increased, the hydrogen and the mixed oil are fully reacted, and the hydrogen supply index of the obtained coal direct liquefaction hydrogen supply solvent is improved.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (10)
1. A washing oil and direct coal-to-liquid oil mixing processing system is characterized by comprising: the system comprises a micro-interface generator, a reaction container, a feeding unit and a processing unit for reacting the obtained mixture; wherein the content of the first and second substances,
the micro-interface generator is connected with the feeding unit, the number of the micro-interface generator is more than or equal to 1, and the micro-interface generator is used for converting pressure energy of hydrogen and/or kinetic energy of mixed oil formed by washing oil and direct coal liquefaction oil into surface energy of hydrogen bubbles, so that the hydrogen bubbles are crushed into micron-sized bubbles with the diameter of 1 mu m or more and d less than 1mm to improve the mass transfer area between the mixed oil and the hydrogen, reduce the thickness of a liquid film and reduce mass transfer resistance, the mixed oil and the micron-sized bubbles are mixed to form a gas-liquid emulsion after crushing, the mass transfer efficiency and the reaction efficiency between the mixed oil and the hydrogen are enhanced within a preset operating condition range, and the micron-sized bubbles and the mixed oil form the gas-liquid emulsion, so that the mass transfer area between the hydrogen and the mixed oil is increased, the hydrogen and the mixed oil are fully reacted, and the hydrogen supply index of the obtained direct;
the reaction container is connected with the micro-interface generator and is used for providing a place for the reaction of the hydrogen and the mixed oil;
the feeding unit is used for conveying the hydrogen and the mixed oil into the micro-interface generator;
and the treatment unit of the mixture obtained by the reaction is connected with the reaction container and is used for treating the mixture obtained after the reaction in the reaction container is finished.
2. The wash oil and coal direct liquefaction oil blending processing system of claim 1, wherein said micro-interface generator is selected from one or more of a pneumatic micro-interface generator, a hydraulic micro-interface generator, and a gas-liquid linkage micro-interface generator.
3. The washing oil and coal direct liquefied oil mixing and processing system according to claim 2, wherein when the number of the micro interface generators is two or more, each micro interface generator is arranged in series and/or in parallel.
4. The wash oil and coal direct liquefaction oil blending processing system of claim 1, wherein said feed unit comprises: a hydrogen storage tank, an oil washing storage tank and a direct coal liquefaction oil storage tank; wherein the content of the first and second substances,
the hydrogen storage tank is connected with the micro-interface generator and is used for providing hydrogen;
the washing oil storage tank is connected with the micro-interface generator and is used for providing washing oil;
the coal direct liquefaction oil storage tank is connected with the micro-interface generator and is used for providing the coal direct liquefaction oil.
5. The wash oil and coal direct liquefaction oil blending processing system of claim 1, wherein said processing unit of the reaction resultant mixture comprises: a separation tank, a rectifying tower and a product collecting tank; wherein the content of the first and second substances,
the separation tank is connected with the reaction container and is used for carrying out gas-liquid separation on the mixture, and after part of the separated hydrogen is discharged, the rest hydrogen is introduced into the micro-interface generator to provide hydrogen for the hydrogenation reaction of the mixed oil and the direct coal liquefaction oil;
the rectifying tower is connected with the separating tank and used for dividing the liquid separated by the separating tank into: light distillate, medium distillate and heavy distillate;
the product collecting tank is connected with the rectifying tower and is used for collecting products.
6. The wash oil and coal direct liquefaction oil blending processing system of claim 5, wherein said product collection tank comprises: a hydrogen donor solvent collection tank and a crude oil collection tank; wherein the content of the first and second substances,
the hydrogen donor solvent collection tank is connected with the rectifying tower and is used for collecting a hydrogen donor solvent consisting of the medium distillate oil and the heavy distillate oil;
the crude oil collecting tank is connected with the rectifying tower and is used for collecting crude oil formed by mixing the medium distillate oil and the light distillate oil.
7. A method for mixing and processing wash oil and coal direct liquefied oil is characterized by comprising the following steps:
(a) mixing a certain amount of washing oil and a certain amount of direct coal liquefaction oil, and introducing the mixture into a micro-interface generator;
(b) introducing a certain amount of hydrogen into the micro-interface generator, wherein the micro-interface generator converts pressure energy of the hydrogen and/or kinetic energy of mixed oil formed by washing oil and coal direct liquefaction oil into surface energy of hydrogen bubbles, so that the hydrogen bubbles are crushed into micron-sized bubbles, and the micron-sized bubbles and the mixed oil form a gas-liquid emulsion;
(c) introducing the gas-liquid emulsion into a reaction container, and fully reacting mixed oil contained in the gas-liquid emulsion with hydrogen under the catalytic action of a catalyst;
(d) introducing the mixture obtained after the reaction into a separation tank for gas-liquid separation, discharging a part of the separated hydrogen, introducing the rest hydrogen into the micro-interface generator again to provide hydrogen for the hydrogenation reaction of the mixed oil and the direct coal liquefaction oil, and introducing the separated liquid into a rectifying tower;
(e) dividing the liquid in the rectifying tower into: the method comprises the steps of mixing light distillate oil, medium distillate oil and heavy distillate oil, introducing the mixture into a crude oil collection tank, and introducing the mixture of the medium distillate oil and the heavy distillate oil into a hydrogen supply solvent collection tank.
8. The method for mixing and processing wash oil and coal direct liquefaction oil as claimed in claim 7, wherein the volume ratio of said mixed oil to said hydrogen gas is 200-1000.
9. The method for mixing and processing wash oil and coal direct liquefaction oil as claimed in claim 7, wherein the reaction temperature in the reaction vessel in step (c) is 320 ℃ to 400 ℃.
10. The method as claimed in claim 7, wherein the reaction pressure in the reaction vessel in step (c) is 2.0 MPa-10.0 MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910600385.8A CN112175650A (en) | 2019-07-04 | 2019-07-04 | System and method for mixing and processing wash oil and direct coal liquefied oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910600385.8A CN112175650A (en) | 2019-07-04 | 2019-07-04 | System and method for mixing and processing wash oil and direct coal liquefied oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112175650A true CN112175650A (en) | 2021-01-05 |
Family
ID=73914629
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910600385.8A Pending CN112175650A (en) | 2019-07-04 | 2019-07-04 | System and method for mixing and processing wash oil and direct coal liquefied oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112175650A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102049220A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Method for enhancing gas-liquid mass transfer of ebullated bed hydrogenation reactor |
| CN102051207A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Method for enhancing mass transfer through suspension bed hydrogenation technology |
| CN102517071A (en) * | 2011-12-26 | 2012-06-27 | 神华集团有限责任公司 | Method for mixing and processing wash oil and direct coal liquefaction oil |
| CN107346378A (en) * | 2017-08-30 | 2017-11-14 | 南京大学 | Micro-interface enhanced reactor mass transfer rate structure imitates regulation-control model modeling method |
-
2019
- 2019-07-04 CN CN201910600385.8A patent/CN112175650A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102049220A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Method for enhancing gas-liquid mass transfer of ebullated bed hydrogenation reactor |
| CN102051207A (en) * | 2009-10-27 | 2011-05-11 | 中国石油化工股份有限公司 | Method for enhancing mass transfer through suspension bed hydrogenation technology |
| CN102517071A (en) * | 2011-12-26 | 2012-06-27 | 神华集团有限责任公司 | Method for mixing and processing wash oil and direct coal liquefaction oil |
| CN107346378A (en) * | 2017-08-30 | 2017-11-14 | 南京大学 | Micro-interface enhanced reactor mass transfer rate structure imitates regulation-control model modeling method |
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 | |
| CN109679690A (en) | A kind of liquid-phase hydrogenatin system and liquid phase hydrogenating method | |
| CN210674823U (en) | Wash oil and direct liquefied coal oil mixed processing system | |
| CN111495288A (en) | Up-down opposite-impact type micro-interface enhanced reaction device and method | |
| CN109679682A (en) | A kind of molten hydrogen storage equipment and molten hydrogen methods | |
| CN106479562B (en) | A kind of dissolving method and application for strengthening hydrogen in reformed oil | |
| CN111686653A (en) | Hydrogenation reaction system of micro-interface enhanced fluidized bed | |
| CN111686646A (en) | Gasoline hydrodesulfurization modification micro-interface enhanced reaction system and method | |
| CN210176791U (en) | Coal and biomass multistage liquefaction system | |
| WO2020186641A1 (en) | Micro-interface enhanced wax oil hydrogenation reaction system and method | |
| CN112175650A (en) | System and method for mixing and processing wash oil and direct coal liquefied oil | |
| CN111686647A (en) | Micro-interface reinforced lubricating oil hydrofining reaction system and method | |
| CN210045220U (en) | Side-mounted micro-interface enhanced reaction device for residual oil hydrogenation reaction | |
| CN111482142A (en) | Underneath type gas-liquid reinforced emulsification fixed bed reaction device and method | |
| CN109679684B (en) | Liquid phase hydrogenation reaction system and method | |
| CN111495287A (en) | Side-mounted micro-interface enhanced reaction device and method for residual oil hydrogenation reaction | |
| CN111482135A (en) | Side gas-liquid reinforced emulsification fixed bed reaction device and method | |
| CN111482145A (en) | Upper-mounted micro-interface enhanced reaction device and method for residual oil hydrogenation reaction | |
| CN112175667A (en) | Mixed oil hydrogenation micro-interface enhanced reaction system and method | |
| CN213506759U (en) | Enhanced reaction system for direct coal liquefaction | |
| CN111686651A (en) | Micro-interface reinforced suspension bed hydrogenation reaction system and method | |
| CN111482136A (en) | Overhead gas-liquid reinforced emulsification fixed bed reaction device and method | |
| CN112175656A (en) | Suspension bed enhanced reaction system and method for direct coal liquefaction | |
| CN115322810B (en) | Heavy oil enhanced hydrogen mixing hydrogenation process, liquid phase hydrogenation reaction system and convection rotary mixer thereof |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210105 |