CN108745224B - Sectional type microreactor device - Google Patents
Sectional type microreactor device Download PDFInfo
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- CN108745224B CN108745224B CN201810637347.5A CN201810637347A CN108745224B CN 108745224 B CN108745224 B CN 108745224B CN 201810637347 A CN201810637347 A CN 201810637347A CN 108745224 B CN108745224 B CN 108745224B
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- adsorber
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- heat exchange
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- 239000012530 fluid Substances 0.000 claims abstract description 31
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- 239000000463 material Substances 0.000 claims abstract description 4
- 239000003463 adsorbent Substances 0.000 claims abstract 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 46
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 21
- FAIAAWCVCHQXDN-UHFFFAOYSA-N phosphorus trichloride Chemical compound ClP(Cl)Cl FAIAAWCVCHQXDN-UHFFFAOYSA-N 0.000 claims description 14
- ONRKUGHFZWYUJP-UHFFFAOYSA-N methylphosphane dihydrochloride Chemical compound Cl.Cl.PC ONRKUGHFZWYUJP-UHFFFAOYSA-N 0.000 claims description 8
- 239000012535 impurity Substances 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims 1
- 238000007789 sealing Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 31
- 239000006096 absorbing agent Substances 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 2
- 238000001179 sorption measurement Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 11
- 239000000047 product Substances 0.000 description 8
- 238000010586 diagram Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- IAJOBQBIJHVGMQ-UHFFFAOYSA-N 2-amino-4-[hydroxy(methyl)phosphoryl]butanoic acid Chemical compound CP(O)(=O)CCC(N)C(O)=O IAJOBQBIJHVGMQ-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- 239000005561 Glufosinate Substances 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 239000011230 binding agent Substances 0.000 description 2
- 208000012839 conversion disease Diseases 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000000110 cooling liquid Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- ZBMRKNMTMPPMMK-UHFFFAOYSA-N 2-amino-4-[hydroxy(methyl)phosphoryl]butanoic acid;azane Chemical compound [NH4+].CP(O)(=O)CCC(N)C([O-])=O ZBMRKNMTMPPMMK-UHFFFAOYSA-N 0.000 description 1
- 238000010146 3D printing Methods 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 239000005562 Glyphosate Substances 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 238000000231 atomic layer deposition Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003115 biocidal effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000007859 condensation product Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- XDDAORKBJWWYJS-UHFFFAOYSA-N glyphosate Chemical compound OC(=O)CNCP(O)(O)=O XDDAORKBJWWYJS-UHFFFAOYSA-N 0.000 description 1
- 229940097068 glyphosate Drugs 0.000 description 1
- 230000002363 herbicidal effect Effects 0.000 description 1
- 239000004009 herbicide Substances 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 238000003754 machining Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- FIKAKWIAUPDISJ-UHFFFAOYSA-L paraquat dichloride Chemical compound [Cl-].[Cl-].C1=C[N+](C)=CC=C1C1=CC=[N+](C)C=C1 FIKAKWIAUPDISJ-UHFFFAOYSA-L 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
- 230000009885 systemic effect Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
- C07F9/00—Compounds containing elements of Groups 5 or 15 of the Periodic Table
- C07F9/02—Phosphorus compounds
- C07F9/28—Phosphorus compounds with one or more P—C bonds
- C07F9/50—Organo-phosphines
- C07F9/52—Halophosphines
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00873—Heat exchange
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00905—Separation
- B01J2219/00909—Separation using filters
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00905—Separation
- B01J2219/00918—Separation by adsorption
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/0095—Control aspects
- B01J2219/00952—Sensing operations
- B01J2219/00954—Measured properties
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The invention relates to a fluid mixing technology, and provides an absorber (13) which is provided with a fluid inlet and a fluid outlet, is internally filled with an adsorption material, and is externally wound with a heating pipe (54). The invention also proposes a combined device of adsorbers, comprising: a microchannel reactor (11) and an absorber (13) which are connected together, wherein the microchannel reactor (11) is provided with a plurality of microchannels, and a heating pipe is wound on the outer surface of the microchannel reactor (11); the adsorber (13) has a fluid inlet and outlet, is internally filled with an adsorbent material, and has a heating tube (54) wrapped around its outer surface. The invention provides a novel device capable of quickly heating two fluids and carrying out reaction.
Description
Technical Field
The present invention relates to fluid reaction technology, and more particularly, to a segmented microreactor device.
Background
Glufosinate is a high-efficiency, low-toxicity and nonselective (biocidal) contact-killing type organophosphorus herbicide with partial systemic effect, and is first developed by Hoechst company in Germany, and has the trade name of Basta and is a racemic mixture. With the emergence of glyphosate resistant weeds and paraquat strong toxicity problems, glufosinate has received wide attention. Among these, the synthesis of the intermediate methylphosphine dichloride is the most critical step in the synthesis of glufosinate.
Disclosure of Invention
In view of the problems in the background art, the invention provides a micro-reactor and an absorber for synthesis. The invention adopts a direct synthesis method, namely methane gas and phosphorus trichlorideThen reacting at 600 ℃ to produce the methyl phosphine dichloride. We designed the present reactor for the first step. The reaction equation is: CH (CH) 4 +PCl 3 →HCl+CH 3 PCl 2 。
The invention proposes a segmented microreactor device comprising: a microchannel reactor and an adsorber connected together, the microchannel reactor having a plurality of microchannels, the microchannel reactor having a heating tube wrapped around its outer surface; the adsorber is provided with a fluid inlet and a fluid outlet, the inside of the adsorber is filled with an adsorption material, and a heating pipe is wound on the outer surface of the adsorber.
Optionally, the segmented microreactor device further comprises: a conduit filter disposed before the microchannel reactor, the microchannel reactor disposed before the adsorber.
Optionally, the conduit filter has at least two fluid inlets.
Optionally, the microchannel reactor has mesh openings to filter impurities.
Optionally, the fluid inlet and outlet of the adsorber have screens to block activated carbon.
Optionally, the channel filter, microchannel reactor and adsorber are sealingly connected by threads.
Optionally, the segmented microreactor means comprises at least two groups of microreactors, each group of microreactors comprising: a microchannel reactor and an adsorber connected in sequence.
Optionally, each set includes a conduit filter disposed before the microchannel reactors of the set.
Optionally, the microreactor groups are connected sequentially.
Optionally, granular activated carbon is fully distributed in the adsorber.
The invention has the beneficial effect of providing a novel device capable of rapidly reacting two fluids.
Drawings
FIG. 1 is a schematic structural diagram of a reaction system according to the present invention.
FIG. 2 is a schematic structural view of an embodiment of the reaction apparatus in FIG. 1.
FIG. 3 is a cross-sectional view of the reaction apparatus of FIG. 2.
FIG. 4 is a schematic structural view of an embodiment of the reaction apparatus in FIG. 1.
FIG. 5 is a cross-sectional view of the reaction apparatus of FIG. 4.
Fig. 6 is a perspective view of the microchannel reactor of fig. 5.
Fig. 7 is a schematic structural diagram of the microstructure apparatus of fig. 1.
Fig. 8 is a schematic structural diagram of a portion of the microstructure apparatus of fig. 7.
Fig. 9 is a schematic structural diagram of a portion of the microstructure apparatus of fig. 7.
Fig. 10 is a schematic structural view of the microstructure apparatus and collection container of fig. 1.
FIG. 11 is a schematic view of the reactor, microstructure apparatus and collection vessel of FIG. 1.
Reference numerals
The first vessel 1, the second vessel 2, the first heat exchanger 3, the second heat exchanger 4, the reaction device 5, the first inlet line 51, the second inlet line 52, the outlet line 53, the compressor 6, the microstructure device 7, the first heat exchange section 71, the second heat exchange section 72, the third heat exchange section 73, the heat exchange line 74, the fluid line 75, the collection line 76, the liquid level meter 8, the automatic hydraulic valve 9, the collection vessel 10, the microchannel reactor 11, the line filter 12, the adsorber 13, the heat exchanger 14.
Detailed Description
Embodiments of the present invention will now be described with reference to the drawings, wherein like elements are designated by like reference numerals. The following embodiments and technical features in the embodiments may be combined with each other without collision.
The present invention is described by way of example in the manufacture of glufosinate-ammonium intermediate methylphosphine dichloride, but the present invention is not limited thereto.
As shown in fig. 1, the reaction system of the present invention comprises a first container 1 for holding a first fluid, such as phosphorus trichloride, the outlet of the first container 1 being provided with a pump through which phosphorus trichloride in the first container 1 is pumped into a pipeline. The second vessel 2 is for a first fluid, such as methane, and preferably a flow meter is provided at the outlet of the second vessel 2 to meter the amount of methane output.
The first container 1 is connected by a pipe to a first heat exchange section 71 of the microstructure apparatus 7 and the second container 2 is connected by a pipe to a second heat exchange section 72 of the microstructure apparatus 7. The fluids in the second vessel 1 and the second vessel 2 are connected to the second heat exchanger 4 and the first heat exchanger 3, respectively, by pipes after heat exchange by the microstructure apparatus 7.
The first heat exchanger 3 and the second heat exchanger 4 may be resistance heaters. In the first heat exchanger 3 and the second heat exchanger 4, phosphorus trichloride and methane were heated to 600 ℃ respectively, both being gases. The first heat exchanger 3 and the second heat exchanger 4 are respectively connected to a first input pipeline 51 and a second input pipeline 52 of the reaction device 5, and phosphorus trichloride and methane react in the reaction device 5 to generate a reaction product methyl phosphine dichloride, and meanwhile, excessive methane exists. The output conduit 53 of the reaction device 5 is connected to the fluid channel 75 of the microstructure device 7.
The reaction apparatus 5 is described in detail below, and fig. 2 shows a perspective view of one embodiment of the reaction apparatus. FIG. 3 shows a cross-sectional view of the reaction apparatus.
The reaction device 5 may be an adsorber 13, the adsorber 13 is a tubular reactor with a diameter of 3cm, the first input pipe 51 is fed with heated methane, the second input pipe 52 is fed with heated phosphorus trichloride, and the fluid pipe 53 outputs the reaction products methyl phosphine dichloride and excess methane. The adsorber 13 is filled with granular activated carbon. Because HCl gas can be generated in the reaction process of the methyl phosphine dichloride and the methane, and the extraction of the product can be influenced unnecessarily, the high-temperature activated carbon 55 is adopted as an acid binding agent to adsorb the HCl gas, and meanwhile, the activated carbon can adsorb a reactant methane, so that the contact area of the methane and the phosphorus trichloride can be increased, and the effect of improving the reaction conversion rate can be achieved. The adsorber 13 is wrapped around the heating tube 54 outside the tube so that the reaction temperature is kept at 600 ℃.
Fig. 4 to 5 show another embodiment of a reaction apparatus comprising a tubular adsorber 13 having a diameter of 3cm and a microchannel reactor 11 having a diameter of 1.5cm, which are alternately combined, and divided into 4 sections in total, the first section and the third section being the tubular adsorber 13, and the second section and the fourth section being the microchannel reactor 11. The tubular adsorber 13 and the microchannel reactor 11 are screwed together by nuts. The tubular adsorber 13 is filled with special granular activated carbon, and has the same structure as the adsorber shown in fig. 2 to 3. The tubular absorber 13 is formed by twisting two parts, is convenient to disassemble periodically, is wound with a heating pipe outside, and efficiently transfers heat to the reaction fluid through a micro-channel. With good temperature control, shorter reaction times to increase yield.
The microchannel reactor 11 is internally provided with a plurality of channels. So that the fluids can be thoroughly mixed in the microchannel reactor 11, the circled portion of fig. 5 shows a cross-sectional view of the microchannel reactor 11, and fig. 6 shows a perspective view of the microchannel reactor 11. The microchannel reactor 11 is internally provided with a plurality of microchannels for rapid heat exchange of fluids. The microchannel reactor 11 may also be wrapped around a heating tube and evenly distributed over the sides of the square microchannel so that the fluid can begin the preliminary reaction.
Optionally, a pipe filter 12 is installed in front of each microchannel reactor 11, and the pipe filter 12 has a mesh in cross section to filter impurities. The two channels of the pipeline filter 12 are respectively filled with methane and phosphorus trichloride, and the methane and the phosphorus trichloride react to obtain reaction products of methyl phosphine dichloride and excessive methane. HCl gas can be generated in the reaction process, the movement of the reaction balance is limited, and the high-temperature activated carbon in the tubular adsorber 13 is used as an acid binding agent to adsorb the HCl gas, so that the reaction balance is promoted to right. Meanwhile, the active carbon can adsorb reactant methane, so that the contact area of methane and phosphorus trichloride can be increased, and the effect of improving the reaction conversion rate is achieved. In addition, a filter screen is provided at the product outlet of the tubular adsorber 13 to block the outflow of activated carbon.
The microstructure apparatus 7 will be described in detail below, and fig. 7 shows a schematic structure of the microstructure apparatus 7, fig. 8 shows a partially enlarged view of the microstructure apparatus 7, and fig. 9 shows a schematic size diagram in fig. 8.
The product from adsorber 13 is fed with excess methane to microstructure device 7. Microstructure device 7 may be made by 3D printing techniques. The microstructure device 7 is a three-section hollow structure, the heat exchange channels of each section are of a layered structure, the fluid channels and the heat exchange channels are staggered, and the fluid channels penetrate through the whole microstructure device 7, as shown in fig. 5.
Specifically, the microstructure apparatus 7 includes a first heat exchange section 71, a second heat exchange section 72, and a third heat exchange section 73. Each section has a diameter of about 2cm. Each heat exchange section comprises a heat exchange channel 74 and a fluid channel 75 which are arranged in a staggered manner in an upper-lower layer, and the heat exchange channel 74 is connected to the first container 1 and is used for inputting phosphorus trichloride to play a role of condensing products. Similarly, the heat exchange channels of the second heat exchange section 72 are connected to the second vessel 2 for feeding methane, functioning as condensation products. The heat exchange channel of the third heat exchange section 73 is used for inputting cooling liquid, and plays a role of condensing products and further cooling the reaction products. In one embodiment, the sheet-like fluid channels 75 may be spaced 500 μm apart, the heat exchange channels 74 may be square tubing having a side length of 400 μm, the heat exchange channels 74 may be spaced 200 μm apart from the sheet-like fluid channels 75, and the spacing between the two heat exchange channels 74 may be 400 μm. Because of the plurality of micro-channels within the microstructure device 7, the interface of the individual lines connected to the microstructure device 7 may be a special one-to-many joint, i.e. a thick line fan-shaped diffusion, branching into a plurality of dimensional channels.
After the fluid in the first and second containers 1, 2 reaches the microstructure device 7, it is heated to a temperature close to the reaction temperature, i.e. 300 c, due to the heat exchange by means of the first and second heat exchange sections 71, 72. Further, when reaching the adsorber 13, the reaction temperature was 600℃so as to be more likely to be heated. At the same time, the fluid channel 53 from the adsorber 13 is output through the fluid conduit 75 of the microstructure device 7 so that the heat of the reactant at approximately 600 c output from the adsorber 13 is transferred to the phosphorus trichloride and methane transferred from the first vessel 1 and the second vessel 2. Therefore, the whole loop forms a closed loop system, and the reactants are preheated while cooling the products, so that a large amount of heat energy is saved.
The total length of the heat exchange parts (the first heat exchange section, the second heat exchange section and the third heat exchange section) of the microstructure device 7 is 10cm, the width and the height are 3cm respectively, 20 layers of layered runners can be arranged, and 21 layers of heat exchange pipelines can be arranged.
As shown in fig. 7, the microstructure apparatus 7 further comprises a collection tube 76, the collection tube 76 being connected to the third heat exchange section 73.
As shown in FIGS. 1 and 11, the reaction system of the present invention further comprises a collecting vessel 10, wherein the collecting vessel 10 is a cavity, the cavity is divided into two parts, and the lower half part is a cup-shaped structure with a diameter of 15cm and a height of 25cm, and the collecting vessel is manufactured by machining. The bottom of the collecting container 10 is provided with a liquid level meter 8, and the outlet is provided with a hydraulic valve 9. When the liquid product reaches a certain liquid level in the collecting container 10, the hydraulic valve 9 is opened, the liquid product flows out of the cavity through the pipeline, and when the liquid level is lowered below the liquid level meter 8, the hydraulic valve 9 is closed, so that methane gas and the product are prevented from flowing out together. The upper half of the collection vessel 10 is flanged to the lower half, the upper half being a plurality of cylindrical heat exchangers 14, the heat exchangers 14 being configured like the first heat exchange sections 71 of the microstructure apparatus 7. The heat exchanger is hollow and densely provided with micropores with the diameter of 300 mu m, the height is 2cm, and the side surface of the heat exchanger 14 is also injected with normal-temperature cooling liquid to further condense gas products which are not condensed in time, and excessive methane is recovered through the structure, heated and then output to the first heat exchanger 3 through the compressor 6 to participate in the reaction again.
In one experiment of the invention, the mixed gas of phosphorus trichloride gas and methane gas is heated to 600 ℃, and the stay time is 5 minutes under normal pressure, so that the conversion rate of the phosphorus trichloride is 100%, and the yield is 68%.
Preferably, the reaction device 5, the microstructure device 7, the microchannel reactor 11, the pipe filter 12, the adsorber 13 are coated for corrosion protection by atomic layer deposition techniques after the formation as described above.
The above embodiments are only preferred embodiments of the present invention, and it is intended that the common variations and substitutions made by those skilled in the art within the scope of the technical solution of the present invention are included in the scope of the present invention.
Claims (3)
1. A segmented microreactor device for producing methylphosphine dichloride, comprising:
comprising at least two sets of sequentially connected microreactor groups, each set of microreactor groups comprising: a pipe filter (12), a microchannel reactor (11) and an adsorber (13) which are connected together in sequence and are connected in a sealing manner by threads,
two channels of the pipeline filter (12) are respectively filled with methane and phosphorus trichloride, and the cross section of the pipeline filter (12) is provided with sieve holes for filtering impurities;
the microchannel reactor (11) is provided with a plurality of microchannels, and a heating pipe is wound on the outer surface of the microchannel reactor (11); the adsorber (13) has a fluid inlet and outlet, is internally filled with an adsorbent material, and has a heating tube (54) wrapped around its outer surface.
2. The segmented microreactor device according to claim 1, wherein,
the fluid inlet and outlet of the adsorber (13) have screens to block activated carbon.
3. The segmented microreactor device according to claim 1, wherein,
granular activated carbon is fully distributed in the adsorber (13).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810637347.5A CN108745224B (en) | 2018-06-20 | 2018-06-20 | Sectional type microreactor device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810637347.5A CN108745224B (en) | 2018-06-20 | 2018-06-20 | Sectional type microreactor device |
Publications (2)
| Publication Number | Publication Date |
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| CN108745224A CN108745224A (en) | 2018-11-06 |
| CN108745224B true CN108745224B (en) | 2023-10-27 |
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|---|---|---|---|---|
| CN101128257A (en) * | 2004-11-12 | 2008-02-20 | 万罗赛斯公司 | Process using microchannel technology for conducting alkylation or acylation reaction |
| CN104332083A (en) * | 2014-10-31 | 2015-02-04 | 徐州工程学院 | Adsorbent adsorption-regeneration presentation device and presentation method thereof |
| CN106215828A (en) * | 2016-09-23 | 2016-12-14 | 中国科学院上海高等研究院 | A kind of microchannel reaction unit, microchannel response system and the method preparing alkene |
| CN106831327A (en) * | 2016-12-14 | 2017-06-13 | 王宇栋 | A kind of pressure control technique that gasification produces methyl alcohol with microreactor combination at a high speed |
| CN108043133A (en) * | 2017-12-15 | 2018-05-18 | 天津普洛普斯科技有限公司 | A kind of micro- reactor off-gas clarifier of environment-friendly type |
| CN208679114U (en) * | 2018-06-20 | 2019-04-02 | 华北电力大学 | A kind of segmented microreactor combination unit based on 3D printing |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6969505B2 (en) * | 2002-08-15 | 2005-11-29 | Velocys, Inc. | Process for conducting an equilibrium limited chemical reaction in a single stage process channel |
| US7250074B2 (en) * | 2003-08-29 | 2007-07-31 | Velocys, Inc. | Process for separating nitrogen from methane using microchannel process technology |
| US7540475B2 (en) * | 2005-09-16 | 2009-06-02 | Battelle Memorial Institute | Mixing in wicking structures and the use of enhanced mixing within wicks in microchannel devices |
-
2018
- 2018-06-20 CN CN201810637347.5A patent/CN108745224B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101128257A (en) * | 2004-11-12 | 2008-02-20 | 万罗赛斯公司 | Process using microchannel technology for conducting alkylation or acylation reaction |
| CN104332083A (en) * | 2014-10-31 | 2015-02-04 | 徐州工程学院 | Adsorbent adsorption-regeneration presentation device and presentation method thereof |
| CN106215828A (en) * | 2016-09-23 | 2016-12-14 | 中国科学院上海高等研究院 | A kind of microchannel reaction unit, microchannel response system and the method preparing alkene |
| CN106831327A (en) * | 2016-12-14 | 2017-06-13 | 王宇栋 | A kind of pressure control technique that gasification produces methyl alcohol with microreactor combination at a high speed |
| CN108043133A (en) * | 2017-12-15 | 2018-05-18 | 天津普洛普斯科技有限公司 | A kind of micro- reactor off-gas clarifier of environment-friendly type |
| CN208679114U (en) * | 2018-06-20 | 2019-04-02 | 华北电力大学 | A kind of segmented microreactor combination unit based on 3D printing |
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| CN108745224A (en) | 2018-11-06 |
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