CN214763480U - Defoaming device and reaction system - Google Patents
Defoaming device and reaction system Download PDFInfo
- Publication number
- CN214763480U CN214763480U CN202120232599.7U CN202120232599U CN214763480U CN 214763480 U CN214763480 U CN 214763480U CN 202120232599 U CN202120232599 U CN 202120232599U CN 214763480 U CN214763480 U CN 214763480U
- Authority
- CN
- China
- Prior art keywords
- conveying pipeline
- defoaming
- conveying
- gas
- pressure
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 21
- 239000002518 antifoaming agent Substances 0.000 claims abstract description 31
- 230000000694 effects Effects 0.000 claims abstract description 18
- 239000012530 fluid Substances 0.000 claims abstract description 15
- 239000002994 raw material Substances 0.000 claims abstract description 11
- 230000009467 reduction Effects 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 38
- 239000000463 material Substances 0.000 claims description 18
- 239000013530 defoamer Substances 0.000 claims description 2
- 238000000926 separation method Methods 0.000 abstract description 14
- 239000000126 substance Substances 0.000 abstract description 8
- 239000000203 mixture Substances 0.000 abstract description 7
- 230000006837 decompression Effects 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 230000000052 comparative effect Effects 0.000 description 17
- 238000001816 cooling Methods 0.000 description 17
- 239000007789 gas Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 11
- 238000003860 storage Methods 0.000 description 10
- 238000005984 hydrogenation reaction Methods 0.000 description 6
- 239000003921 oil Substances 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 230000008859 change Effects 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 239000012752 auxiliary agent Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 238000010791 quenching Methods 0.000 description 3
- 238000004364 calculation method Methods 0.000 description 2
- 238000004581 coalescence Methods 0.000 description 2
- 230000008602 contraction Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- 239000002199 base oil Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 230000005501 phase interface Effects 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000006557 surface reaction Methods 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Landscapes
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The utility model relates to a chemical industry equipment technical field particularly, relates to a fire fighting equipment and reaction system. The defoaming device comprises a first conveying pipeline for conveying a raw material to be defoamed, a second conveying pipeline for conveying a defoaming agent and a pressure reduction structure for reducing the pressure of the mixed fluid by utilizing the Venturi effect; the pressure reducing structure, the first conveying pipeline and the second conveying pipeline are provided with inlet ends and outlet ends opposite to the inlet ends, and the outlet ends of the first conveying pipeline and the second conveying pipeline are communicated with the inlet ends of the pressure reducing structure. Through waiting defoaming raw materials and defoaming agent all carry to the decompression structure in, utilize the venturi effect to produce pressure effect to the fluid mixture, utilize pressure variation to make its inside production low pressure state in the twinkling of an eye, make the bubble inflation gather and merge, guaranteed final separation effect, can realize gathering fast and clearing up of bubble.
Description
Technical Field
The utility model relates to a chemical industry equipment technical field particularly, relates to a fire fighting equipment and reaction system.
Background
In petroleum refining and chemical production, gas-liquid-solid three-phase contact reaction is often involved, in the three-phase contact reaction, surface reaction occurs among three phases, the reaction speed is high, the intrinsic kinetics of the reaction is not a rate control step of the whole reaction process, and the influence of the internal and external diffusion of reactants and the mass transfer process is large. In order to improve the reaction rate and relax the reaction conditions, the mass transfer process is enhanced by methods of enhancing fluid disturbance, thinning a boundary layer, enlarging a gas-liquid phase interface and the like. The method for constructing the micro interface system between gas and liquid by crushing the gas reaction phase into micron-scale bubbles has the advantages of strong operability, good mass transfer strengthening effect and the like, and has wide application prospect in the oil refining industry, particularly in the hydrogenation field.
The micro-interface strengthening technology is applied to the petroleum hydrogenation process, and the high gas content rate of the constructed reaction gas-liquid phase micro-interface flow can still be ensured after the flow passes through a plurality of components of a feeding system, such as a heating furnace, a bent pipe and the like. This in turn presents another problem: the hydrogen volume that provides in the oil hydrogenation reaction process is far more than the hydrogen volume that actual reaction consumed, and like this after the reaction finishes, still there are a large amount of hydrogen microbubbles to exist in the product oil, produces the influence to downstream splitter's normal operation, and the throughput is reduced to light, and the steady operation of whole equipment is influenced to the weight. Therefore, there is an urgent need for a method for defoaming unreacted hydrogen bubbles at the product outlet, which can rapidly coalesce and destroy the microbubbles by destroying the stability of the bubbles, thereby achieving the purpose of gas-liquid separation.
In view of this, the present application is specifically made.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a fire fighting equipment, it can carry out the speed to the bubble in the gas-liquid mixture and go out.
An object of the utility model is to provide a reaction system, it can carry out the defoaming to the mixture after the reaction fast.
The embodiment of the utility model is realized like this:
the utility model provides a defoaming device, which comprises a first conveying pipeline for conveying raw materials to be defoamed, a second conveying pipeline for conveying a defoaming agent and a pressure reduction structure for reducing the pressure of mixed fluid by utilizing Venturi effect; the pressure reducing structure, the first conveying pipeline and the second conveying pipeline are provided with inlet ends and outlet ends opposite to the inlet ends, and the outlet ends of the first conveying pipeline and the second conveying pipeline are communicated with the inlet ends of the pressure reducing structure.
In the preferred embodiment of the present invention, the pressure reducing structure is a venturi tube.
In the preferred embodiment of the present invention, the outlet end of the second conveying pipeline is connected to the middle pipeline of the first conveying pipeline, and the outlet end of the first conveying pipeline is connected to the inlet end of the pressure reducing structure.
In the preferred embodiment of the present invention, the cooling device further comprises a cooler, the cooler has a cooling material inlet and a cooling material outlet, and the outlet end of the venturi tube is communicated with the cooling material inlet of the cooler.
In a preferred embodiment of the present invention, the cooler is a shell-and-tube heat exchanger.
In the preferred embodiment of the present invention, the cooling device further comprises a gas-liquid separator, and the cooling material outlet of the cooler is communicated with the feed inlet of the gas-liquid separator.
In the preferred embodiment of the present invention, the top of the gas-liquid separator is connected to a gas conveying pipeline, and the bottom of the gas-liquid separator is connected to a liquid conveying pipeline.
In the preferred embodiment of the present invention, the system further comprises a defoaming agent storage, and the discharge port of the defoaming agent storage is communicated with the inlet end of the second conveying pipeline.
The utility model discloses in the preferred embodiment, still including the pump body that is used for providing transport power, the discharge gate of defoaming agent memory passes through the pump body with the entrance point of second conveying line and communicates.
The utility model also provides a reaction system, including above-mentioned fire fighting equipment.
The embodiment of the utility model provides a beneficial effect is: through waiting defoaming raw materials and defoaming agent all carry to the decompression structure in, utilize the venturi effect to produce pressure effect to the fluid mixture, utilize pressure variation to make its inside production low pressure state in the twinkling of an eye, make the bubble inflation gather and merge, guaranteed final separation effect, can realize gathering fast and clearing up of bubble.
The utility model discloses can utilize the chemical action of auxiliary agent and venturi's pressure variation's combined action to realize gathering fast and clearing up of microbubble, be suitable for and use in reaction system, utilize above-mentioned fire fighting equipment to carry out the defoaming with the material after reacting to obtain very good separation effect.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are required to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention, and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
Fig. 1 is a schematic structural diagram of a defoaming device provided in an embodiment of the present invention;
fig. 2 is a schematic structural diagram of the defoaming device provided by the comparative example of the present invention.
The icon is 100-defoaming device; 101-a first delivery line; 102-a second delivery line; 110-antifoam reservoir; 120-a pump body; 130-a pressure reducing structure; 140-a cooler; 150-a gas-liquid separator; 151-gas delivery line; 152-liquid delivery line; 160-cyclone separation tank.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention, as generally described and illustrated in the figures herein, may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the accompanying drawings, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.
In the description of the present invention, it should be noted that the terms "upper", "lower", "inner", "outer", and the like indicate the position or positional relationship based on the position or positional relationship shown in the drawings, or the position or positional relationship which is usually placed when the utility model is used, and are only for convenience of description and simplification of the description, but do not indicate or imply that the device or element to be referred must have a specific position, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "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 meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Referring to fig. 1, an embodiment of the present invention provides a defoaming apparatus 100, including a first conveying pipeline 101 for conveying a raw material to be defoamed, a second conveying pipeline 102 for conveying a defoaming agent, and a depressurization structure 130 for depressurizing a mixed fluid by using a venturi effect; the depressurization structure 130, the first conveying pipe 101, and the second conveying pipe 102 each have an inlet end and an outlet end opposite to the inlet end, and the outlet ends of the first conveying pipe 101 and the second conveying pipe 102 communicate with the inlet end of the depressurization structure 130.
It should be noted that, the first conveying pipeline 101 conveys the raw material to be defoamed, such as a reacted mixture, into the depressurization structure 130, the second conveying pipeline 102 conveys the defoaming agent into the depressurization structure 130, the raw material to be defoamed and the defoaming agent are depressurized in the depressurization structure 130 by using a venturi effect, and an instant low-pressure state is generated in the raw material to be defoamed and the defoaming agent by using pressure change, so that bubbles are expanded and coalesced.
In a preferred embodiment, the outlet end of the second conveying pipe 102 is connected to the middle pipe of the first conveying pipe 101, and the outlet end of the first conveying pipe 101 is connected to the inlet end of the pressure reducing structure 130. In this way, before entering the pressure reducing structure 130, the mixing of the raw material to be defoamed and the defoaming agent is realized, and chemical defoaming is performed.
In some embodiments, the pressure reducing structure 130 may be a venturi tube, i.e., a venturi mixer, which is used to generate a momentary low pressure state inside the mixed material, so that the bubbles are expanded and coalesced. Controlling the diameter of the contraction section of the Venturi tube, and controlling the Reynolds number of the micro-bubble flow to be 5 multiplied by 10 when the micro-bubble flow flows through the contraction section by combining the material properties of the micro-bubble flow5～5×106In the meantime. The pressure reducing structure 130 may also be other devices that can reduce the pressure of the mixed fluid by using the venturi effect.
The raw material component to be defoamed in the first transfer line 101 is not limited, and may be a mixed fluid in which an organic solvent is in a liquid phase and which has a need for defoaming. In some embodiments, the mixture after the hydrogenation reaction of petroleum can be effectively removed with the defoaming device 100.
The defoaming agent in the second conveying pipeline 102 is specifically selected according to the application environment, and in the hydrogenation of distillate oil in petrochemical industry, a water-soluble silicon-free defoaming agent is preferred, and the defoaming agent is not limited in other organic matter systems.
In the preferred embodiment of the present invention, the system further comprises an antifoaming agent storage 110, wherein the discharge port of the antifoaming agent storage 110 is communicated with the inlet end of the second conveying pipeline 102, and the antifoaming agent storage 110 is used for temporarily storing the antifoaming agent, so as to facilitate the continuous access.
In some embodiments, the defoamer memory 110 is a tank structure such as a storage tank for storing in the chemical field.
In some embodiments, a pump body 120 is further included for providing a conveying power, the discharge port of the anti-foam agent storage 110 is communicated with the inlet port of the second conveying pipeline 102 through the pump body 120, and the conveying power is provided by the pump body 120 to convey the anti-foam agent in the anti-foam agent storage 110 to the second conveying pipeline 102 and then to the pressure reduction structure 130. Specifically, the pump body 120 may be a general centrifugal pump, and the structure thereof is not described in detail.
In the preferred embodiment of the present invention, the cooling device 140 is further included, the cooling device 140 has an inlet for cooling material and an outlet for cooling material, and the outlet end of the venturi tube (i.e. the pressure reducing structure 130) is communicated with the inlet for cooling material of the cooling device 140. And further cooling the mixed material to reduce the gas solubility so as to further remove gas and realize defoaming.
In some embodiments, the cooler 140 is a quench structure to achieve rapid cooling, and may be any type of efficient heat exchange method that controls the temperature difference of the micro-bubble flow entering and exiting the quench device to be not less than 40 ℃. Preferably, the cooler 140 is a quenching device formed by a shell-and-tube heat exchanger, and the cooling medium is preferably circulating liquid or other cooling liquid in the reaction, so as to ensure that the temperature difference of the micro-bubble flow at the cooling material inlet and the cooling material outlet of the cooler 140 reaches above 40 ℃.
In the preferred embodiment of the present invention, after the triple functions of the micro bubble fast extinguishing aid, the venturi tube and the cooler 140, it can be ensured that most of the bubbles in the micro bubble flow are gathered and broken, and the gas-liquid mixture can enter the gas-liquid separator 150 for fast separation. Specifically, the cooled material outlet of the cooler 140 is communicated with the feed port of the gas-liquid separator 150 to perform gas-liquid separation of the mixed fluid. The gas-liquid separator 150 is a general chemical device for realizing gas-liquid separation, and the specific structure thereof is not described herein.
In some embodiments, a gas delivery line 151 is connected to the top of the gas-liquid separator 150, a liquid delivery line 152 is connected to the bottom of the gas-liquid separator 150, the top output gas is vented or delivered to other processes through the gas delivery line 151 after passing through the gas-liquid separator 150, and the bottom output liquid is delivered to other processes through the liquid delivery line 152.
The embodiment of the utility model provides a still provide a reaction system, including above-mentioned fire fighting equipment 100, can also include the reactor, the misce bene of reactor output gets into fire fighting equipment 100 and carries out the defoaming.
Specifically, the reactor may be a reactor for a general petroleum hydrogenation reaction.
The embodiment of the utility model provides a still provide a method for eliminate microbubble in microbubble stream fast, it adopts the device in fig. 1 to go on, and concrete step is as follows:
(1) the microbubble flow carrying gas in the liquid phase comes from the upstream of the application scene, enters the first conveying pipeline 101, is injected with the microbubble fast extinguishing auxiliary agent quantitatively by the pump body 120 before entering the venturi tube (namely, the pressure reduction structure 130), is mixed with the microbubble flow, and carries out chemical defoaming to a certain extent on part of the microbubbles.
(2) The microbubble mixed with the microbubble fast extinguishing auxiliary agent (i.e. the defoaming agent) flows into the Venturi tube, and the flowing state of fluid flowing through the Venturi tube is controlled through the change of the pipe diameter, so that the pressure inside the Venturi tube is changed at the same time of fast change of the speed, and the stability of the microbubble flow is damaged under the two actions of the defoaming agent and the pressure change, so that the coalescence and the digestion of bubbles are promoted.
(3) The micro-bubble flow enters the cooler 140 for cooling, and the temperature difference of the micro-bubble flow at the inlet and the outlet of the cooler 140 is ensured to reach more than 40 ℃.
After the triple actions of (1) to (3), the coalescence and the crushing of most bubbles in the micro-bubble flow can be ensured, and the gas-liquid mixed phase enters the gas-liquid separator 150 for rapid separation.
The embodiment of the utility model provides an advantage lies in: traditional gas-liquid separation device majority is used for separating in the great and unstable application environment of existence of bubble yardstick, is difficult to realize the quick separation who stabilizes little bubble flow fast, and the utility model discloses a chemistry defoaming, temperature and three kinds of modes of pressure sudden change act on the little bubble flow of bubble size at 1 ~ 1000 mu m within range, destroy the stability of even little bubble flow through chemical bond force, heating power and mechanical force, promote the microbubble growth, strengthen its striking and gather and the probability, realize breaking out fast of microbubble and the double-phase quick separation of gas-liquid.
The present invention will be described in detail with reference to the following embodiments.
Example 1
The embodiment adopts the bubble removal device 100 in fig. 1 to perform bubble removal and rapid gas-liquid separation on the formed micro-bubble flow. The defoaming device 100 includes a defoaming agent storage 110, a pump body 120, a venturi tube, a cooler 140, and a gas-liquid separator 150.
Hydrogen is mixed in diesel oil in a microbubble mode with the diameter of 50-500 mu m through a microbubble generator set to prepare a microbubble flow with the gas content of 45%, and the microbubble flow is heated to 350 ℃ and then enters a first conveying pipeline 101 in the attached drawing. The microbubble mixed flow is firstly mixed with the microbubble quick-extinguishing auxiliary agent conveyed by the second conveying pipeline 102, the antifoaming agent is the medium federal B-266 antifoaming agent, and the injection amount is 25 mu g/g relative to the feeding amount.
The mixed fluid enters into the Venturi tube, and the Reynolds number of the fluid is 5 x 10 by controlling the throat in the Venturi tube5On the left and right sides, a momentary low pressure is formed inside, so that a large amount of dissolved gas is precipitated and then contacts with bubbles to coalesce, enlarge and break. Then the micro-bubble flow enters a cooler 140 (a tubular heat exchanger), cold water is used as a heat exchange medium, and the temperature difference between the inlet and the outlet of the cooler 140 is controlled to be 50 ℃, namely the temperature of the micro-bubble flow flowing out of the quencher is 300 ℃. The quenched micro-bubble flow enters the gas-liquid separator 150 for rapid separation, and the liquid at the bottom of the gas-liquid separator 150 is taken to test the fluid density and calculate the defoaming rate, and the results are shown in table 1.
Comparative example 1:
the comparative example used the same microbubble quick-extinguishing aid as in example 1, and the same injection amount for defoaming test, and the microbubble defoaming rate was measured, and the results are shown in table 1.
Comparative example 2:
in the comparative example, the rotational flow type mechanical defoaming was adopted, the micro-bubble flow with the same bubble size and gas content rate was subjected to rotational flow treatment, and the defoaming rate was measured, and the results are shown in table 1.
Comparative example 3:
in this comparative example, the venturi section of example 1 was replaced with a cyclone, and the front end thereof was filled with a wire mesh filler, and the defoaming rate thereof was measured, and the results are shown in Table 1. The apparatus used in this comparative example is shown in FIG. 2 and includes an antifoaming agent storage 110, a pump body 120, a cyclone 160, a cooler 140, and a gas-liquid separator 150.
Test example 1
The defoaming effect after the treatment of the methods in example 1 and comparative examples 1 to 3 was tested, and the results are shown in table 1.
The test method comprises the following steps: the defoaming effect in the examples and comparative examples was defined by the defoaming ratio of microbubbles, i.e., the percentage of the amount of gas after defoaming and the total amount of gas before defoaming, and the calculation was performed by measuring the density of the fluid before and after defoaming, and the calculation formula was as follows:
wherein, PtTo eliminate oil density (100 ℃, kg/m) after micro-bubbles3)；
P0To eliminate the density (100 ℃, kg/m) of oil before micro-bubbles3)；
PjDensity (100 ℃, kg/m) of base oil product3)。
TABLE 1 test results of defoaming Effect of examples and comparative examples
| Group of | Example 1 | Comparative example 1 | Comparative example 2 | Comparative example 3 |
| Defoaming rate | 99.7％ | 34.6％ | 21.3％ | 79.5％ |
As can be seen from Table 1, the defoaming device 100 provided by the present invention has significant advantages in removing micro-bubble flow with a diameter of 50-500 μm. In comparative example 3, its main removal thinking is in basic agreement with the utility model discloses, therefore the microbubble defoaming rate is also obviously higher than two other comparative examples, but comparative example 3's defoaming effect will be inferior to example 1.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A defoaming device is characterized by comprising a first conveying pipeline for conveying a raw material to be defoamed, a second conveying pipeline for conveying a defoaming agent and a pressure reduction structure for reducing the pressure of a mixed fluid by utilizing a Venturi effect; the pressure reducing structure, the first conveying pipeline and the second conveying pipeline are provided with inlet ends and outlet ends opposite to the inlet ends, and the outlet ends of the first conveying pipeline and the second conveying pipeline are communicated with the inlet ends of the pressure reducing structure.
2. The bubble removal apparatus of claim 1, wherein the pressure reducing structure is a venturi tube.
3. The bubble removal apparatus of claim 2, wherein the outlet end of the second delivery line is connected to an intermediate line of the first delivery line, and the outlet end of the first delivery line is connected to the inlet end of the pressure reducing structure.
4. The defoaming apparatus according to claim 2, further comprising a cooler having a material to be cooled inlet and a material to be cooled outlet, the outlet end of the venturi tube communicating with the material to be cooled inlet of the cooler.
5. The bubble removal apparatus of claim 4, wherein the cooler is a shell and tube heat exchanger.
6. The defoaming apparatus according to claim 4, further comprising a gas-liquid separator, wherein the cooled material outlet of the cooler is communicated with a feed inlet of the gas-liquid separator.
7. The defoaming apparatus according to claim 6, wherein a gas conveying pipeline is connected to the top of the gas-liquid separator, and a liquid conveying pipeline is connected to the bottom of the gas-liquid separator.
8. The defoaming apparatus of claim 1, further comprising a defoamer reservoir, a discharge port of which communicates with the inlet end of the second conveying line.
9. The defoaming apparatus of claim 8, further comprising a pump body for providing a conveying power, wherein the outlet of the defoaming agent reservoir is in communication with the inlet end of the second conveying line through the pump body.
10. A reaction system comprising the bubble removal apparatus of any one of claims 1-9.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120232599.7U CN214763480U (en) | 2021-01-27 | 2021-01-27 | Defoaming device and reaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120232599.7U CN214763480U (en) | 2021-01-27 | 2021-01-27 | Defoaming device and reaction system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214763480U true CN214763480U (en) | 2021-11-19 |
Family
ID=78750274
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120232599.7U Active CN214763480U (en) | 2021-01-27 | 2021-01-27 | Defoaming device and reaction system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214763480U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115646364A (en) * | 2022-11-01 | 2023-01-31 | 中国石油化工股份有限公司 | Reaction device for olefin hydroformylation reinforced by micro-bubble flow and application |
| CN115650833A (en) * | 2022-11-01 | 2023-01-31 | 中国石油化工股份有限公司 | Process method for enhancing olefin hydroformylation by micro bubble flow |
-
2021
- 2021-01-27 CN CN202120232599.7U patent/CN214763480U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115646364A (en) * | 2022-11-01 | 2023-01-31 | 中国石油化工股份有限公司 | Reaction device for olefin hydroformylation reinforced by micro-bubble flow and application |
| CN115650833A (en) * | 2022-11-01 | 2023-01-31 | 中国石油化工股份有限公司 | Process method for enhancing olefin hydroformylation by micro bubble flow |
| CN115650833B (en) * | 2022-11-01 | 2024-04-16 | 中国石油化工股份有限公司 | Process method for strengthening olefin hydroformylation by microbubble flow |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN210045215U (en) | Low-pressure gas-liquid reinforced emulsion bed reaction device | |
| CN214763480U (en) | Defoaming device and reaction system | |
| US4931225A (en) | Method and apparatus for dispersing a gas into a liquid | |
| US4861352A (en) | Method of separating a gas and/or particulate matter from a liquid | |
| KR0173996B1 (en) | Apparatus for dissolving a gas into and mixing the same with a liquid | |
| CN109679682B (en) | Hydrogen dissolving equipment and hydrogen dissolving method | |
| JP2004075771A (en) | Apparatus for producing gas hydrate | |
| WO2023284030A1 (en) | Instant dewatering dmc preparation system and preparation method | |
| WO2020155505A1 (en) | Low-pressure gas-liquid enhanced emulsifying bed reaction device and method | |
| JP7180085B2 (en) | Pressurized reactor and method for leaching valuable metals using the same | |
| CN107098317B (en) | System and method for producing hydrogen peroxide by anthraquinone process | |
| Oyevaar et al. | Mass transfer phenomena and hydrodynamics in agitated gas—Liquid reactors and bubble columns at elevated pressures: State of the art | |
| JP2001523154A (en) | Method and apparatus for contacting ozone with a fluid to be treated, especially water | |
| US8486233B2 (en) | Apparatus, process and system for delivering fluid to a distillation column or reactor | |
| CN216024809U (en) | 2-methyl tetrahydrofuran's micro-interface preparation system | |
| CN114471300B (en) | Microchannel assembly, microchannel mixing device, mixing system and application | |
| CN106277150B (en) | Air flotation microbubble aerating device for petroleum water treatment and using method thereof | |
| US10603643B2 (en) | Process and device for dispersing gas in a liquid | |
| CN213644075U (en) | Microbubble generator and hydrocarbon oil hydrogenation reactor | |
| EP3463608B1 (en) | Method for the de-aeration of froths and foams | |
| CN101678299A (en) | Hydrogen-oxygen blender-distributor | |
| CN111167385B (en) | Jet type gas-liquid reactor for preparing acid by utilizing aldehyde raw material and air | |
| CN215480657U (en) | System for preparing DMC (dimethyl carbonate) by methanol carbonylation | |
| CN115040900B (en) | Device and method for strengthening micro-bubble separation by using rotational flow centrifugal force field | |
| CN220506696U (en) | Deaerator and deoxidization system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |