CN112058185A - Reaction system and method for petroleum resin hydrogenation - Google Patents
Reaction system and method for petroleum resin hydrogenation Download PDFInfo
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- CN112058185A CN112058185A CN202010828604.0A CN202010828604A CN112058185A CN 112058185 A CN112058185 A CN 112058185A CN 202010828604 A CN202010828604 A CN 202010828604A CN 112058185 A CN112058185 A CN 112058185A
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 129
- 239000011347 resin Substances 0.000 title claims abstract description 83
- 229920005989 resin Polymers 0.000 title claims abstract description 83
- 239000003208 petroleum Substances 0.000 title claims abstract description 81
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000001257 hydrogen Substances 0.000 claims abstract description 104
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 104
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 103
- 239000002994 raw material Substances 0.000 claims abstract description 42
- 239000003054 catalyst Substances 0.000 claims abstract description 35
- 239000007791 liquid phase Substances 0.000 claims description 33
- 239000007789 gas Substances 0.000 claims description 28
- 239000012071 phase Substances 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 23
- 238000000926 separation method Methods 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 4
- 238000005191 phase separation Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 239000007792 gaseous phase Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 23
- 230000000694 effects Effects 0.000 description 11
- 239000000203 mixture Substances 0.000 description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 229910052759 nickel Inorganic materials 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000005728 strengthening Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- YAIQCYZCSGLAAN-UHFFFAOYSA-N [Si+4].[O-2].[Al+3] Chemical compound [Si+4].[O-2].[Al+3] YAIQCYZCSGLAAN-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 229920006272 aromatic hydrocarbon resin Polymers 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000005501 phase interface Effects 0.000 description 1
- 229910001404 rare earth metal oxide Inorganic materials 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
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Classifications
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- 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
- B01J8/04—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 the fluid passing successively through two or more beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/02—Foam dispersion or prevention
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F8/00—Chemical modification by after-treatment
- C08F8/04—Reduction, e.g. hydrogenation
Abstract
The invention provides a reaction system and a method for petroleum resin hydrogenation, wherein the reaction system comprises: a pre-hydrogenation reactor provided with a plurality of catalyst beds; a micro-interface generator is arranged between catalyst beds inside the pre-hydrogenation reactor; the side wall of the pre-hydrogenation reactor is respectively provided with a raw material inlet and a hydrogen inlet, hydrogen enters the micro-interface generator from the hydrogen inlet after being preheated by the hydrogen preheater, and the raw material petroleum resin solution enters the micro-interface generator from the raw material inlet after being preheated by the raw material preheater. The reaction system provided by the invention is combined with the micro-interface generator, so that the energy consumption is reduced, the reaction temperature is reduced, the reaction yield is improved, the utilization rate of raw materials is improved, particularly the utilization rate of hydrogen is improved, and the productivity is effectively improved.
Description
Technical Field
The invention relates to the field of petroleum resin hydrogenation, in particular to a reaction system and a reaction method for petroleum resin hydrogenation.
Background
Petroleum resin is an important basic chemical raw material and one of important organic chemical products which are developed rapidly in recent years. The C9 petroleum resin contains high unsaturated bonds, and is easy to react under the action of oxygen and other chemical substances, so that the application of the petroleum resin is greatly limited, and the petroleum resin needs to be hydrotreated.
The C9 petroleum resin has a relatively large molecular weight (200-3000), and can realize a good hydrogenation effect only when the operation conditions reach 10-20 MPa and 230-300 ℃ under the catalysis of a high-activity catalyst. In addition, the C9 petroleum resin also contains toxic impurities such as sulfur, nitrogen and the like, and the catalyst is easy to deactivate, so that the industrialization of the C9 petroleum resin is difficult.
At present, three hydrogenation processes of C9 petroleum resin are mainly adopted, namely a slurry bed hydrogenation process, a trickle bed hydrogenation process and a spray bed hydrogenation process. The traditional C9 petroleum resin hydrogenation process generally has the following problems:
(1) the slurry bed loop reactor hydrogenation technology is suitable for small-scale production, the separation difficulty of reaction products and catalysts is high, the separated catalysts can adsorb partial products, and the catalyst loss is high.
(2) The trickle bed hydrogenation process has high reaction pressure (about 20MPa), high investment cost and operation cost of the device and reduced intrinsic safety.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The first purpose of the invention is to provide a reaction system for petroleum resin hydrogenation, which is based on a micro-interface reaction strengthening technology, takes C9 resin and a solvent as continuous phases, efficiently crushes hydrogen into micron-sized bubbles through a micro-interface generator, disperses the micron-sized bubbles into a resin solution to form a micro-interface system, improves the gas-liquid phase interface area in a hydrogenation reactor by tens of times, greatly improves the mass transfer rate from the gas phase to the reaction liquid and the macroscopic hydrogenation rate, and further can reduce the original reaction pressure, reaction temperature and catalyst usage amount, thereby developing a high-efficiency and energy-saving reaction system for micro-interface strengthening C9 petroleum resin hydrogenation.
The second purpose of the invention is to provide a reaction method for hydrogenating petroleum resin by adopting the reaction system, the hydrogenated petroleum resin obtained by the reaction is environment-friendly and clean, the application is wide, the application range of the petroleum resin is improved, and the method is worthy of wide popularization and application.
In order to achieve the above purpose of the present invention, the following technical solutions are adopted:
the invention provides a reaction system for petroleum resin hydrogenation, which comprises: a pre-hydrogenation reactor provided with a plurality of catalyst beds;
a micro-interface generator is arranged between the catalyst beds inside the pre-hydrogenation reactor; the side wall of the pre-hydrogenation reactor is respectively provided with a raw material inlet and a hydrogen inlet, hydrogen enters the micro-interface generator from the hydrogen inlet after being preheated by the hydrogen preheater, a raw material petroleum resin solution enters the micro-interface generator from the raw material inlet after being preheated by the raw material preheater, and the hydrogen and the petroleum resin solution are dispersed and crushed in the micro-interface generator to form micro-bubbles;
and introducing the hydrogenation product reacted from the pre-hydrogenation reactor into a first hot high-pressure separator for gas-liquid phase separation, introducing the separated liquid phase into a refined hydrogenation reactor for further hydrogenation, and recycling the separated gas phase.
According to the reaction system for petroleum resin hydrogenation, the micro-interface generator is arranged in the hydrogenation reactor, and the entering hydrogen is dispersed and crushed into micro bubbles, so that the mass transfer effect is improved.
Preferably, the reaction system comprises a circulating hydrogen channel and a new hydrogen channel, the circulating hydrogen channel and the new hydrogen channel are converged into a total hydrogen channel, the total hydrogen channel is divided into three branch channels, and the first branch channel is preheated by a raw material preheater after being mixed with the raw material petroleum resin solution and then enters the micro-interface generator from the raw material inlet;
the second branch channel enters the micro-interface generator from the hydrogen inlet after being preheated by the hydrogen preheater;
the third branch channel is directly led into the micro-interface generator in the pre-hydrogenation reactor.
Preferably, two catalyst beds are arranged in the refined hydrogenation reactor, and a micro-interface generator is respectively arranged between the two catalyst beds and the bottom of the refined hydrogenation reactor; the micro interface generator positioned at the upper part in the refined hydrogenation reactor receives hydrogen from the third branch passage, and the micro interface generator positioned at the lower part in the refined hydrogenation reactor receives a liquid phase from the bottom of the first hot high-pressure separator and hydrogen from the second branch passage after being preheated by the hydrogen preheater.
The invention arranges the micro-interface generator in the pre-hydrogenation reactor and the refined hydrogenation reactor, and the hydrogen enters into the reactor in three branches, so the hydrogen enters into the micro-interface generator in different modes, especially in the refined hydrogenation reactor, the number of the micro-interface generator arranged in the refined hydrogenation reactor is exactly two because the number of the catalyst bed layers arranged in the refined hydrogenation reactor is two, the number of the micro-interface generator arranged between the catalyst bed layers and the bottom of the reactor is exactly two, the micro-interface generator is arranged from top to bottom in sequence, the micro-interface generator positioned at the upper part mainly enters into the gas phase which is not preheated, the micro-interface generator positioned at the bottom mainly enters into the hydrogen which is preheated and the liquid phase, because the liquid phase feeding of the micro-interface generator at the bottom is more convenient, the mass transfer effect can be improved after the preheated gas phase and the liquid phase are mixed together, the side part of the micro-interface generator positioned at the upper part is, the device mainly plays a role in assisting the micro-interface generator at the bottom to improve the effect of dispersing and crushing together, so that gas-phase feeding is gas phase which is not required to be preheated, and the upper and lower micro-interface generators are matched together to play a role in crushing and dispersing the micro-interface. The micro-interface generator on the upper part forms a secondary micro-interface system to realize the mixing and strengthening reaction with the unreacted petroleum resin solution.
In addition, the mode of hydrogen entering in the pre-hydrogenation reactor is the same as the mode of hydrogen entering in the refined hydrogenation reactor, one part of hydrogen enters without preheating, and the other part of hydrogen enters to be preheated, so that the mode not only reduces the energy consumption, but also ensures the effect of micro-interface crushing and dispersion. In addition, in order to improve the mixing effect of the hydrogen and the raw materials, a part of the hydrogen enters from the first branch passage to be mixed with the raw material petroleum resin solution so as to enhance the hydrogenation reaction effect.
The micro-interface generators arranged in the pre-hydrogenation reactor and the refined hydrogenation reactor are of a pneumatic type, and hydrogen and petroleum resin are introduced into the micro-interface generators and then dispersed and crushed, so that the subsequent hydrogenation reaction is enhanced, impurities such as sulfur, nitrogen and the like are removed, and the mass transfer effect is improved.
It will be appreciated by those skilled in the art that the micro-interface generator used in the present invention is described in the prior patents of the present inventor, such as the patents of application nos. CN201610641119.6, 201610641251.7, CN201710766435.0, CN106187660, CN105903425A, CN109437390A, CN205833127U and CN 207581700U. The detailed structure and operation principle of the micro bubble generator (i.e. micro interface generator) is described in detail in the prior patent CN201610641119.6, which describes that "the micro bubble generator comprises a body and a secondary crushing member, wherein the body is provided with a cavity, the body is provided with an inlet communicated with the cavity, the opposite first end and second end of the cavity are both open, and the cross-sectional area of the cavity decreases from the middle of the cavity to the first end and second end of the cavity; the secondary crushing member is disposed at least one of the first end and the second end of the cavity, a portion of the secondary crushing member is disposed within the cavity, and an annular passage is formed between the secondary crushing member and the through holes open at both ends of the cavity. The micron bubble generator also comprises an air inlet pipe and a liquid inlet pipe. "the specific working principle of the structure disclosed in the application document is as follows: liquid enters the micro-bubble generator tangentially through the liquid inlet pipe, and gas is rotated at a super high speed and cut to break gas bubbles into micro-bubbles at a micron level, so that the mass transfer area between a liquid phase and a gas phase is increased, and the micro-bubble generator in the patent belongs to a pneumatic micro-interface generator.
In addition, the first patent 201610641251.7 describes that the primary bubble breaker has a circulation liquid inlet, a circulation gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker communicates the feed inlet with the gas-liquid mixture outlet, which indicates that the bubble breakers all need to be mixed with gas and liquid, and in addition, as can be seen from the following drawings, the primary bubble breaker mainly uses the circulation liquid as power, so that the primary bubble breaker belongs to a hydraulic micro-interface generator, and the secondary bubble breaker simultaneously introduces the gas-liquid mixture into an elliptical rotating ball for rotation, thereby realizing bubble breaking in the rotating process, so that the secondary bubble breaker actually belongs to a gas-liquid linkage micro-interface generator. In fact, the micro-interface generator is a specific form of the micro-interface generator, whether it is a hydraulic micro-interface generator or a gas-liquid linkage micro-interface generator, however, the micro-interface generator adopted in the present invention is not limited to the above forms, and the specific structure of the bubble breaker described in the prior patent is only one of the forms that the micro-interface generator of the present invention can adopt. Furthermore, the prior patent 201710766435.0 states that the principle of the bubble breaker is that high-speed jet flows are used to achieve mutual collision of gases, and also states that the bubble breaker can be used in a micro-interface strengthening reactor to verify the correlation between the bubble breaker and the micro-interface generator; moreover, in the prior patent CN106187660, there is a related description on the specific structure of the bubble breaker, see paragraphs [0031] to [0041] in the specification, and the accompanying drawings, which illustrate the specific working principle of the bubble breaker S-2 in detail, the top of the bubble breaker is a liquid phase inlet, and the side of the bubble breaker is a gas phase inlet, and the liquid phase coming from the top provides the entrainment power, so as to achieve the effect of breaking into ultra-fine bubbles, and in the accompanying drawings, the bubble breaker is also seen to be of a tapered structure, and the diameter of the upper part is larger than that of the lower part, and also for better providing the entrainment power for the liquid phase. Since the micro-interface generator was just developed in the early stage of the prior patent application, the micro-interface generator was named as a micro-bubble generator (CN201610641119.6), a bubble breaker (201710766435.0) and the like in the early stage, and is named as a micro-interface generator in the later stage along with the continuous technical improvement, and the micro-interface generator in the present invention is equivalent to the micro-bubble generator, the bubble breaker and the like in the prior art, and has different names.
In summary, the micro-interface generator of the present invention belongs to the prior art, although some bubble breakers belong to the type of pneumatic bubble breakers, some bubble breakers belong to the type of hydraulic bubble breakers, and some bubble breakers belong to the type of gas-liquid linkage bubble breakers, the difference between the types is mainly selected according to the different specific working conditions, and in addition, the connection between the micro-interface generator and the reactor and other equipment, including the connection structure and the connection position, is determined according to the structure of the micro-interface generator, which is not limited.
The catalyst for the hydrogenation reaction is a nickel-based catalyst, preferably a supported nickel-based catalyst, or more preferably a nickel-based catalyst modified by an alkaline earth metal oxide or a rare earth metal oxide, and the carrier is selected from silicon oxide or aluminum oxide.
Preferably, the active component of the catalyst for cracking hydrogenation reaction is oxides of nickel, cobalt and molybdenum, and the carrier is alumina, silicon-aluminum oxide or molecular sieve. The pre-hydrogenation and the refined hydrogenation have the functions of removing impurities such as sulfur, nitrogen and the like, and improve the quality of petroleum resin products.
Preferably, the reaction system further comprises a second hot high-pressure separator, the product after the reaction of the refined hydrogenation reactor is introduced into the second hot high-pressure separator from the top of the refined hydrogenation reactor for gas-liquid phase separation, and the separated liquid phase is cooled by the high-pressure cooler and then sent to the cold low-pressure separator for further separation.
Preferably, the gaseous phase separated from the cold low-pressure separator is returned to the circulating hydrogen passage for reuse, and the liquid phase separated from the cold low-pressure separator is directly collected as a product.
Preferably, the gas phase separated from the first hot high pressure separator and the gas phase separated from the second hot high pressure separator are merged and go to the cold low pressure separator.
Preferably, the reaction system comprises a raw material tank for storing a raw material petroleum resin solution, the raw material tank being connected to the raw material preheater.
And the product from the pre-hydrogenation reactor and the product from the refined hydrogenation reactor are subjected to gas-liquid separation through a hot high-pressure separator positioned at the top of the reactor, the separator can adjust the pressurized pressure according to different separated products, the separated liquid phase finally converges into a cold low-pressure separator for further gas-liquid separation, the separated gas phase also finally converges into the cold low-pressure separator for further gas-liquid separation, the finally formed gas phase can be recycled as circulating hydrogen through the gas-liquid separation of the cold low-pressure separator, and the liquid phase is directly collected as a product.
And the first thermal high-pressure separator performs gas-liquid separation on the reacted product, the obtained liquid phase mixture, the preheated hydrogen and the petroleum resin are mixed and then enter the micro-interface generator to form a micro-interface system, the petroleum resin hydrogenation reaction is performed again, the obtained product is conveyed to the second thermal high-pressure separator, and the gas phase product and the liquid phase product are separated. And cooling the liquid-phase product by a high-pressure cooler and then conveying the liquid-phase product to a cold low-pressure separator to obtain the final product hydrogenated petroleum resin.
The invention also provides a reaction method of the petroleum resin hydrogenation reaction system, which comprises the following steps:
the petroleum resin and hydrogen mixed micro interface is dispersed and crushed, and then is subjected to hydrogenation reaction, separation, hydrocracking, gas-liquid separation and fractionation.
Preferably, the temperature of the hydrogenation reaction is 230-290 ℃, and the pressure of the hydrogenation reaction is 5-18 MPa.
Specifically, the reaction method comprises the steps of breaking hydrogen into micro-bubbles with a micron scale through a micro-interface, releasing the micro-bubbles into the reactor to increase the phase boundary mass transfer area between the hydrogen and the petroleum resin in the hydrogenation process of the petroleum resin, enabling the hydrogen to be in full contact with a resin solution in a micro-bubble state, and enabling a formed micro-interface system to enter a catalyst bed layer to carry out hydrogenation reaction on the petroleum resin.
The product obtained by the hydrogenation reaction of the petroleum resin has good quality and high yield. The reaction method for petroleum resin hydrogenation has low reaction temperature, greatly reduced pressure and high liquid hourly space velocity, which is equivalent to improving the productivity.
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the reaction system for petroleum resin hydrogenation, the micro-interface generator connected with the gas-liquid phase feeding pipeline is arranged in the reactor, so that hydrogen is crushed into micro bubbles with the diameter of more than or equal to 1 mu m and less than 1mm by the micro-interface generator before the hydrogen and the petroleum resin are subjected to petroleum resin hydrogenation reaction, the hydrogen is contacted with methanol in the micro bubble state, the phase boundary mass transfer area between the hydrogen and the petroleum resin is increased in the petroleum resin hydrogenation reaction process, the hydrogen and the petroleum resin are fully mixed and then subjected to petroleum resin hydrogenation reaction, and the problem that the reaction efficiency of the system is reduced due to the fact that the petroleum resin and the hydrogen cannot be fully mixed in the reactor in the prior art is solved;
(2) the reaction system of the invention returns the finally separated hydrogen to the circulating hydrogen channel for reuse, thereby further saving the production cost;
(3) the whole reaction system of the invention carries out gas-liquid separation twice, and can obtain high-purity hydrogenated petroleum resin.
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 reaction system for hydrogenating petroleum resin according to an embodiment of the present invention.
Description of the drawings:
10-a raw material tank; 20-a raw material preheater;
30-a hydrogen preheater; 40-new hydrogen channel;
50-a circulating hydrogen channel;
70-a first branch channel; 80-a second branch channel;
90-a third branch channel; 100-a pre-hydrogenation reactor;
110-a first hot high pressure separator; 120-refining the hydrogenation reactor;
130-a second hot high pressure separator; 140-a micro-interface generator;
150-high pressure cooler; 160-Cold Low pressure separator.
Detailed Description
The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to more clearly illustrate the technical solution of the present invention, the following description is made in the form of specific embodiments.
Examples
Referring to fig. 1, a reaction system for hydrogenation of petroleum resin according to an embodiment of the present invention mainly includes a pre-hydrogenation reactor 100 and a refined hydrogenation reactor 120;
the pre-hydrogenation reactor 100 is a fixed bed reactor, a plurality of catalyst beds are arranged in the pre-hydrogenation reactor, a micro-interface generator 140 is arranged between the catalyst beds, preferably, the number of the catalyst beds is 3, the number of the micro-interface generators 140 is 3, two catalyst beds are arranged in the refined hydrogenation reactor 120, the micro-interface generators 140 are respectively arranged between the two catalyst beds and the bottom of the refined hydrogenation reactor 120, and the number of the micro-interface generators 140 arranged in the refined hydrogenation reactor 120 is 2.
The reaction system comprises a circulating hydrogen channel 50 and a new hydrogen channel 40, wherein the circulating hydrogen channel 50 and the new hydrogen channel 40 converge to form an overall hydrogen channel, the circulating hydrogen channel 50 and the new hydrogen channel 40 are both in a slender round pipe shape, the overall hydrogen channel is divided into three branch channels, namely three branch channels, a raw material inlet and a hydrogen inlet are respectively formed in the side wall of the pre-hydrogenation reactor 100, and the first branch channel 70 is mixed with the raw material petroleum resin solution, preheated by the raw material preheater 20 and then enters the micro-interface generator 140 from the raw material inlet. The raw petroleum resin solution is stored in a raw material tank 10 and, in use, is delivered to a raw material preheater 20 for preheating and ultimately to a micro-interfacial generator 140.
The second branch channel 80 is preheated by the hydrogen preheater 30 and then enters the micro-interface generator 140 from the hydrogen inlet, and at the same time, one branch enters the micro-interface generator 140 located at the lower part inside the refined hydrogenation reactor 120.
The third branch channel 90 is directly introduced into the micro-interface generator 140 in the pre-hydrogenation reactor 100, and simultaneously, a branch is directly introduced into the micro-interface generator 140 located at the upper part inside the refined hydrogenation reactor 120.
The pre-hydrogenation reactor 100 and the refined hydrogenation reactor 120 are used for receiving petroleum resin solution and hydrogen, and at the site where the catalyst bed layer is used as the petroleum resin hydrogenation reaction, the micro-interface generator 140 arranged inside the reactor is used for crushing the hydrogen to form a micro-interface system before the petroleum resin hydrogenation reaction, and the pressure energy of gas and/or the kinetic energy of liquid are/is converted into the surface energy of bubbles and transferred to the bubbles, so that the bubbles are crushed into micro-bubbles with the diameter of more than or equal to 1 μm and less than 1mm, the micro-interface generator 140 is driven by gas, and the input gas amount is far larger than the liquid amount.
The first hot high-pressure separator 110 is connected with the pre-hydrogenation reactor 100, the second hot high-pressure separator 130 is connected with the refined hydrogenation reactor 120, the first hot high-pressure separator 110 and the second hot high-pressure separator 130 are used for separating a gas phase and a liquid phase mixture after a hydrogenation reaction of petroleum resin, the liquid phase separated by the first hot high-pressure separator 110 enters the refined hydrogenation reactor 120 for further hydrogenation reaction, the gas phase separated by the first hot high-pressure separator 110 and the gas phase separated by the second hot high-pressure separator 130 are combined and then go to the cold low-pressure separator 160 for separating raw material hydrogen and product hydrogenated petroleum resin, and finally product hydrogenated petroleum resin is obtained, and the hydrogen returns to the circulating hydrogen channel 50 for reuse. The liquid phase separated in the second hot high pressure separator 130 goes to the high pressure cooler 150 for cooling and then to the cold low pressure separator 160 for separation of the product and the gas phase.
In the above embodiment, in order to increase the dispersion and mass transfer effects, an additional micro-interface generator 140 may be additionally provided, the installation position is not limited, and the micro-interface generator may be external or internal, and may be installed on the side wall inside the kettle in a manner of being arranged relatively when the micro-interface generator is installed internally, so as to realize the opposite collision of micro-bubbles coming out from the outlet of the micro-interface generator 140.
In the above embodiment, the types of the pre-hydrogenation reactor 100 and the refined hydrogenation reactor 120 may be other types such as a fixed bed reactor, a boiling bed reactor, and the like, and the feeding and discharging manner is not limited.
In the above embodiment, the number of the pump bodies is not specifically required, and the pump bodies may be arranged at corresponding positions as required.
The working process and principle of the petroleum resin hydrogenation reaction system of the present invention are briefly described as follows:
the total hydrogen pipeline is connected with the circulating hydrogen channel 50 and the new hydrogen channel 40, and is divided into three branches, petroleum resin solution is conveyed into the reaction system from the raw material tank 10, catalyst is filled into catalyst beds of the pre-hydrogenation reactor 100 and the refined hydrogenation reactor 120, the system is started, the reaction temperature is set to be 230 ℃, and the pressure is set to be 5 MPa.
Mixing the petroleum resin solution from the raw material tank 10 with a small part of mixed hydrogen (a mixture of new hydrogen and circulating hydrogen), heating the mixed hydrogen by a raw material preheater 20, entering a micro-interface generator 140 from the bottom of a pre-hydrogenation reactor 100, mixing the mixed hydrogen with another part of mixed hydrogen heated by a hydrogen preheater 30 in the micro-interface generator 140 to form a micro-interface system, smashing the hydrogen into micro-bubbles by the micro-interface generator 140, releasing the micro-bubbles into the pre-hydrogenation reactor 100, enabling the hydrogen to be fully contacted with the petroleum resin solution in a micro-bubble state, and carrying out petroleum resin hydrogenation reaction on a catalyst bed layer of the pre-hydrogenation reactor 100. The middle section of the catalyst is additionally provided with cold hydrogen which is not preheated, and the cold hydrogen enters the micro-interface generator 140 to be mixed with the petroleum resin solution to form a micro-interface system again.
The reacted mixture enters the first hot high-pressure separator 110 for separation, the separated liquid phase enters the micro-interface generator 140 from the bottom of the refined hydrogenation reactor 120 and forms a micro-interface system with another path of hydrogen mixture heated by the hydrogen preheater 30, the micro-interface generator 140 breaks the hydrogen into micro-bubbles with a micron scale and releases the micro-bubbles into the refined hydrogenation reactor 120, so that the hydrogen is fully contacted with the petroleum resin solution in a micro-bubble state, and the petroleum resin hydrogenation reaction is carried out on a catalyst bed layer of the refined hydrogenation reactor 120. Cold hydrogen is added in the catalyst bed of the refined hydrogenation reactor 120, enters the micro-interface generator 140 and is mixed with the petroleum resin solution, and a micro-interface system is formed again.
The mixture reacted from the refined hydrogenation reactor 120 enters the second hot high-pressure separator 130 for separation, the separated gas phase component enters the subsequent system for recycling, and the liquid phase component enters the high-pressure cooler 150 for cooling and then is conveyed to the cold low-pressure separator 160 for separation. The separated gas-phase product enters a subsequent system for recycling, and the liquid-phase component is the product hydrogenated petroleum resin. The content of the hydrogenated petroleum resin is detected, and the purity reaches 90 percent.
In the reaction process, other operating conditions are unchanged, and when the reaction temperature is set to be 260 ℃, the pressure is set to be 12MPa, and the purity reaches 95 percent.
In the reaction process, other operating conditions are unchanged, and when the reaction temperature is set to 290 ℃, the pressure is set to 18MPa, and the purity reaches 98 percent.
By adopting the hydrogenation reaction process, the purity of the hydrogenated petroleum resin is improved and can reach more than 95%.
In addition, the pressure and the temperature of the hydrogenation reaction kettle are reduced by laying the micro-interface generator, and the energy consumption is fully reduced.
In a word, compared with the reaction system for petroleum resin hydrogenation in the prior art, the reaction system for petroleum resin hydrogenation has the advantages of fewer equipment components, small occupied area, low energy consumption, low cost, high safety, controllable reaction and high raw material conversion rate, is equivalent to providing a reaction system with stronger operability for the field of petroleum resin hydrogenation, and is worthy of wide popularization and application.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (9)
1. A reaction system for petroleum resin hydrogenation is characterized by comprising a pre-hydrogenation reactor provided with a plurality of catalyst beds;
a micro-interface generator is arranged between the catalyst beds inside the pre-hydrogenation reactor; the side wall of the pre-hydrogenation reactor is respectively provided with a raw material inlet and a hydrogen inlet, hydrogen enters the micro-interface generator from the hydrogen inlet after being preheated by the hydrogen preheater, a raw material petroleum resin solution enters the micro-interface generator from the raw material inlet after being preheated by the raw material preheater, and the hydrogen and the petroleum resin solution are dispersed and crushed in the micro-interface generator to form micro-bubbles;
and introducing the hydrogenation product reacted from the pre-hydrogenation reactor into a first hot high-pressure separator for gas-liquid phase separation, introducing the separated liquid phase into a refined hydrogenation reactor for further hydrogenation, and recycling the separated gas phase.
2. The reaction system of claim 1, comprising a circulating hydrogen channel and a new hydrogen channel, wherein the circulating hydrogen channel and the new hydrogen channel are combined into a total hydrogen channel, the total hydrogen channel is divided into three branch channels, and a first branch channel is mixed with the raw petroleum resin solution, preheated by a raw material preheater and enters the micro-interface generator from the raw material inlet;
the second branch channel enters the micro-interface generator from the hydrogen inlet after being preheated by the hydrogen preheater;
the third branch channel is directly led into the micro-interface generator in the pre-hydrogenation reactor.
3. The reaction system of claim 2, wherein two catalyst beds are disposed in the refined hydrogenation reactor, and a micro-interface generator is disposed between the two catalyst beds and the bottom of the refined hydrogenation reactor; the micro interface generator positioned at the upper part in the refined hydrogenation reactor receives hydrogen from the third branch passage, and the micro interface generator positioned at the lower part in the refined hydrogenation reactor receives a liquid phase from the bottom of the first hot high-pressure separator and hydrogen from the second branch passage after being preheated by the hydrogen preheater.
4. The reaction system of claim 2, further comprising a second hot high-pressure separator, wherein the product after the reaction of the refined hydrogenation reactor is introduced into the second hot high-pressure separator from the top of the refined hydrogenation reactor for gas-liquid phase separation, and the separated liquid phase is cooled by the high-pressure cooler and then sent to the cold low-pressure separator for further separation.
5. The reaction system of claim 4, wherein the gaseous phase separated from the cold low pressure separator is returned to the recycle hydrogen channel for reuse and the liquid phase separated from the cold low pressure separator is collected directly as a product.
6. The reaction system of claim 4 wherein the gas phase separated from the first hot high pressure separator and the gas phase separated from the second hot high pressure separator are merged before going to the cold low pressure separator.
7. The reaction system according to any one of claims 1 to 6, wherein the reaction system comprises a raw material tank for storing a raw material petroleum resin solution, the raw material tank being connected to the raw material preheater.
8. The reaction method using the petroleum resin hydrogenation reaction system according to any one of claims 1 to 7, characterized by comprising:
the raw material petroleum resin solution and hydrogen are mixed with a micro interface, dispersed and crushed, then subjected to hydrogenation reaction, and subjected to gas-liquid separation and cooling to obtain a product, and the product is collected.
9. The reaction process as claimed in claim 8, wherein the temperature of the hydrogenation reaction is 230 ℃ and 290 ℃, and the pressure of the hydrogenation reaction is 5-18 MPa.
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| CN202010828604.0A CN112058185A (en) | 2020-08-18 | 2020-08-18 | Reaction system and method for petroleum resin hydrogenation |
| PCT/CN2020/122804 WO2022036837A1 (en) | 2020-08-18 | 2020-10-22 | Reaction system and method for hydrogenation of petroleum resin |
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| CN202010828604.0A CN112058185A (en) | 2020-08-18 | 2020-08-18 | Reaction system and method for petroleum resin hydrogenation |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112940155A (en) * | 2021-01-21 | 2021-06-11 | 张宇 | Preparation process of petroleum resin with high reaction rate and low softening point |
| CN113522177A (en) * | 2021-06-30 | 2021-10-22 | 江苏新化化工有限公司 | Reactor for improving hydration reaction effect of propylene |
| WO2022142326A1 (en) * | 2020-12-28 | 2022-07-07 | 南京延长反应技术研究院有限公司 | Reaction system and method for refining crude terephthalic acid by hydrogenation |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114904458B (en) * | 2022-05-27 | 2024-03-26 | 中国神华煤制油化工有限公司 | High-pressure polyethylene device and pressure control method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105175633A (en) * | 2015-09-08 | 2015-12-23 | 胡平 | Combined hydrotreatment method and hydrotreatment system for petroleum resin |
| CN106554814A (en) * | 2015-09-24 | 2017-04-05 | 中国石油天然气股份有限公司 | Thick C inferior9Fraction multi-stek hydrogenation process for purification |
| JP2017213519A (en) * | 2016-05-31 | 2017-12-07 | 三菱ケミカルエンジニアリング株式会社 | Gas-liquid reaction device having micronanobubble generator and gas-liquid reaction method using the gas-liquid reaction device |
| CN107497372A (en) * | 2016-06-14 | 2017-12-22 | 中国石油天然气集团公司 | Hydrogenation reactor |
| CN110396425A (en) * | 2019-08-20 | 2019-11-01 | 中国石油化工股份有限公司 | Micro-interface strengthens the device and method that liquid phase circulation adds hydrogen |
| CN111359556A (en) * | 2019-03-15 | 2020-07-03 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced hydrogenation reaction system |
| CN111482144A (en) * | 2019-01-29 | 2020-08-04 | 南京延长反应技术研究院有限公司 | Bottom-mounted micro-interface enhanced reaction device and method for residual oil hydrogenation reaction |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3484421A (en) * | 1965-07-20 | 1969-12-16 | Exxon Research Engineering Co | Two stage hydrogenation process (ii) |
| US4540480A (en) * | 1982-10-23 | 1985-09-10 | Arakawa Kagaku Kogyo Kabushiki Kaisha | Process for preparing hydrogenated petroleum resin |
| CN105367714B (en) * | 2015-12-03 | 2018-04-27 | 大连理工大学 | A kind of method for preparing drogenated DCPD resin |
-
2020
- 2020-08-18 CN CN202010828604.0A patent/CN112058185A/en active Pending
- 2020-10-22 WO PCT/CN2020/122804 patent/WO2022036837A1/en active Application Filing
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105175633A (en) * | 2015-09-08 | 2015-12-23 | 胡平 | Combined hydrotreatment method and hydrotreatment system for petroleum resin |
| CN106554814A (en) * | 2015-09-24 | 2017-04-05 | 中国石油天然气股份有限公司 | Thick C inferior9Fraction multi-stek hydrogenation process for purification |
| JP2017213519A (en) * | 2016-05-31 | 2017-12-07 | 三菱ケミカルエンジニアリング株式会社 | Gas-liquid reaction device having micronanobubble generator and gas-liquid reaction method using the gas-liquid reaction device |
| CN107497372A (en) * | 2016-06-14 | 2017-12-22 | 中国石油天然气集团公司 | Hydrogenation reactor |
| CN111482144A (en) * | 2019-01-29 | 2020-08-04 | 南京延长反应技术研究院有限公司 | Bottom-mounted micro-interface enhanced reaction device and method for residual oil hydrogenation reaction |
| CN111359556A (en) * | 2019-03-15 | 2020-07-03 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced hydrogenation reaction system |
| CN110396425A (en) * | 2019-08-20 | 2019-11-01 | 中国石油化工股份有限公司 | Micro-interface strengthens the device and method that liquid phase circulation adds hydrogen |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022142326A1 (en) * | 2020-12-28 | 2022-07-07 | 南京延长反应技术研究院有限公司 | Reaction system and method for refining crude terephthalic acid by hydrogenation |
| CN112940155A (en) * | 2021-01-21 | 2021-06-11 | 张宇 | Preparation process of petroleum resin with high reaction rate and low softening point |
| CN113522177A (en) * | 2021-06-30 | 2021-10-22 | 江苏新化化工有限公司 | Reactor for improving hydration reaction effect of propylene |
| CN113522177B (en) * | 2021-06-30 | 2022-08-16 | 江苏新化化工有限公司 | Reactor for improving hydration reaction effect of propylene |
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|---|---|
| WO2022036837A1 (en) | 2022-02-24 |
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