CN109336052A - For producing micro- reaction system of hydrogen chloride and the hydrogen chloride production method based on the system - Google Patents
For producing micro- reaction system of hydrogen chloride and the hydrogen chloride production method based on the system Download PDFInfo
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- CN109336052A CN109336052A CN201811404363.6A CN201811404363A CN109336052A CN 109336052 A CN109336052 A CN 109336052A CN 201811404363 A CN201811404363 A CN 201811404363A CN 109336052 A CN109336052 A CN 109336052A
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- hydrogen chloride
- micro
- hydrogen
- reaction
- microreactor
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- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 69
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 title claims abstract description 69
- 229910000041 hydrogen chloride Inorganic materials 0.000 title claims abstract description 69
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 58
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 47
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 44
- 239000007789 gas Substances 0.000 claims abstract description 44
- 239000001257 hydrogen Substances 0.000 claims abstract description 44
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 44
- 239000000460 chlorine Substances 0.000 claims abstract description 43
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 39
- 238000001816 cooling Methods 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 66
- 238000000034 method Methods 0.000 claims description 10
- 238000005660 chlorination reaction Methods 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 3
- 230000001351 cycling effect Effects 0.000 claims 1
- 239000000376 reactant Substances 0.000 claims 1
- 230000001737 promoting effect Effects 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 6
- 230000004044 response Effects 0.000 description 5
- 238000004880 explosion Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910002804 graphite Inorganic materials 0.000 description 3
- 239000010439 graphite Substances 0.000 description 3
- 230000020169 heat generation Effects 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 230000004069 differentiation Effects 0.000 description 2
- 239000008246 gaseous mixture Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 229910001504 inorganic chloride Inorganic materials 0.000 description 1
- 239000002085 irritant Substances 0.000 description 1
- 231100000021 irritant Toxicity 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/012—Preparation of hydrogen chloride from the elements
Abstract
The invention discloses a kind of for producing micro- reaction system of hydrogen chloride, it is characterized in that substituting synthetic furnace with microreactor.It furthermore include: that a, hydrogen and chlorine are passed through in micro-mixer and are sufficiently mixed the invention also discloses the hydrogen chloride production method based on the system；B mixed gas enters microreactor and reacts；C, the hydrogen chloride gas that reaction generates obtains product after cooling.The invention has the advantages that 1) hydrogen chloride product purity significantly improves compared with prior art, according to an embodiment of the invention, hydrogen chloride product purity can reach 98% or more；2) micro- reaction system structure for using of the present invention is simple, and only needing same unit device to be arranged in juxtaposition can reach scale mass production purpose, produce it is easy to control, using industrially promoting.
Description
Technical field
The present invention relates to a kind of hydrogen chloride synthesis technologies.
Background technique
Hydrogen chloride, molecular formula HCl are a kind of gas of colourless irritant smell, are made of chlorine atom and hydrogen atom.Its
Aqueous solution is commonly called as hydrochloric acid, relative molecular mass 36.5.Mainly for the preparation of dyestuff, drug, fragrance, organic-inorganic chloride etc..
Usual hydrogen chloride gas is prepared using synthetic furnace, there is steel synthetic furnace, graphitic synthetic furnace, the free air cooling of heat transfer type
But formula and two kinds of water-cooling jacket.Steel synthetic furnace holds corrosion-vulnerable at the top and bottom of furnace, and service life is short, few at present
Enterprise uses.And graphitic synthetic furnace has many advantages, such as corrosion-resistant, high temperature resistant, is the mainstream synthetic furnace of current synthesising hydrogen.Example
As the patent document of the production method of the entitled reagent grade hydrochloric acid of Publication No. CN1640813A describes a kind of compare more typically
The method using graphitic synthetic furnace synthesising hydrogen.Using hydrogen chloride gas purity prepared by graphitic synthetic furnace be usually 91~
94%.
Summary of the invention
For the purity for improving chlorination hydrogen production, the present invention provides a kind of for producing micro- reaction system of hydrogen chloride.
The technical scheme adopted by the invention is that: for producing micro- reaction system of hydrogen chloride, it is characterised in that: including micro-
Reactor, synthetic reaction carry out in microreactor.
The gaseous mixture of hydrogen and chlorine is a kind of explosive gaseous mixture, and explosion limit is 5%~87.5% (volume hundred
Divide ratio), range is very wide.In prior art, the lamp cap that chlorine and hydrogen are passed through graphite furnace simultaneously mixed after with igniting dress
Igniting is set, and since two kinds of gases are there are biggish density variation, it cannot accomplish absolutely to be sufficiently mixed, and graphite furnace volume is big,
Hydrogen molecule is more, chlorine molecule is also more, and contact area is big, and the heat that when burning generates is more, while the production of hydrogen chloride at present
Journey is continuous production process, and hydrogen and chlorine, which constantly enter graphite furnace also, causes the risk of mixed gas part inhomogeneities to increase
Add, if within the scope of explosion limit, the rapid spatial expansion of mixed gas in the confined space is easy to happen explosion.Currently
The generation that technical staff is exploded in order to prevent, generally use the hydrogen that is passed through it is much more excessive than chlorine (molar ratio hydrogen: chlorine=
1.1~1.2:1) mode, in practice it has proved that the program can effectively prevent that safety accident occurs, but this scheme causes simultaneously
Hydrogen content is high and lead to the reduction of chlorination hydrogen purity in chlorination hydrogen production.
In the present invention, inventor is using microreactor substitution graphitic synthetic furnace as synthesizer, due to microreactor
The hydraulic diameter of microchannel is only 0.1~5mm, therefore microreactor device hydrogen is lacked by what pipeline was discharged, with chlorine
Contact area very little is scattered and disappeared quickly even if the heat of generation is few within the scope of explosion limit, will not be exploded；Therefore nothing
It need to ensure hydrogen much excessive the problem of also there is no security risks, it is only necessary to maintain stable reaction to carry out, make hydrogen slightly mistake
Amount, as described above, the reduction of hydrogen ratio is so that therefore product purity is also improved, to realize mesh of the invention
's.Reacting the hydrogen chloride gas generated can be stand-by into hydrogen chloride buffer tank storage after hydrogen chloride cooler is cooling.
In above scheme, since the hydraulic diameter of the microchannel of microreactor is only 0.1~5mm, it is difficult to realize hydrogen
Gas and chlorine are passed through microchannel simultaneously and guarantee that the uniformity in microchannel can stablize progress to guarantee to react, because
This present invention is also provided with micro-mixer, is carried out in advance by the way that hydrogen and chlorine to be passed through in micro-mixer simultaneously by certain flow ratio
Microreactor is entered back into after mixing, to overcome the above problem.
To prevent the temperature of microreactor excessively high, corresponding heat-exchange system can be set, reaction temperature is controlled, hold
Intelligible, the common all kinds of heat-exchange systems in this field, such as circulation can be used in heat-exchange system, and specific arragement construction can
To be designed according to the structure of microreactor, such as a kind of preferred scheme is inventors herein proposed in the present invention: the present invention
Microreactor may include air-tight chamber and the reaction zone that is arranged in air-tight chamber, the reaction zone be provided with to
A few microchannel, and hot water cyclesystem is set simultaneously, hot water cyclesystem includes the air-tightness chamber with microreactor
The circulating hot water upper hose and circulating hot water return pipe of room connection.In the equipment course of work, circulating hot water passes through hot water circuit
The circulating hot water upper hose of system enters in the air-tight chamber of microreactor, the microchannel internal-response object with reaction zone
Indirect heat exchange occurs, is controlled reaction temperature at 1500~2500 DEG C by the hot temperature of control loop and flow, in favor of reaction
It carries out and ensures safety.Hot water cyclesystem can also further be improved, such as increase liquid vapour separation equipment, heat exchange
Circulating hot water afterwards forms steam mixture and passes through hot water cyclesystem recovery section heat as a vapor, and circulating hot water is then
Microreactor is returned to by water supply pipeline to continue to take away heat of reaction, what the heat of recycling can be used for that steam is needed to be heated
Workshop section.
As a further improvement of the present invention, temperature is respectively arranged on the inlet duct and outlet conduit of micro-mixer
Detector and pressure sensor；On-line detector, temperature monitor and pressure is provided on the microreactor outlet conduit to pass
Sensor, the on-line detector include hydrogen chloride purity detecting instrument and free chlorine contents detector；The hydrogen chloride buffer tank is set
It is equipped with pressure sensor；In order to be monitored to production process.
The invention also discloses a kind of methods using micro- reaction system production hydrogen chloride, comprising the following steps:
A, by dry hydrogen and chlorine according to the molar ratio hydrogen of flows per unit time: chlorine=1.01~1.05:1
Ratio is passed through in micro-mixer is sufficiently mixed simultaneously, obtains mixed gas；
B, enter microreactor from the mixed gas that micro-mixer comes out, pass through igniter provocative reaction, mixed gas
Reaction generates hydrogen chloride gas in microchannel, while circulating hot water passes through the circulating hot water upper hose of hot water cyclesystem
Into in the air-tight chamber of microreactor, indirect heat exchange occurs with the microchannel internal-response object of reaction zone, passes through control
Circulating hot water temperature processed and flow control reaction temperature at 1500~2500 DEG C；The mixed gas is in microchannel
It is 5~20s by the time；
C, the hydrogen chloride gas that reaction generates obtains chlorination hydrogen production after cooling.
The production that hydrogen chloride is carried out based on micro- reaction system of the invention can be realized using this method.
The beneficial effects of the present invention are: 1) hydrogen chloride product purity significantly improves compared with prior art, according to the present invention
Embodiment, hydrogen chloride product purity can reach 98% or more；2) micro- reaction system structure that the present invention uses is simple, only needs phase
Being arranged in juxtaposition with cell arrangement can reach scale mass production purpose, and production is easy to control, conducive to industrially promoting.
Detailed description of the invention
Fig. 1 is of the invention for producing micro- reaction system structural schematic diagram of hydrogen chloride.
In the figure, it is marked as 1- micro-mixer, 2- microreactor, 201- air-tight chamber, 202- reaction zone, 3- chlorination are hydrogen-cooled
But device, 4- hydrogen chloride buffer tank, 5- hot water cyclesystem, 501- circulating hot water upper hose, 502- circulating hot water return pipe, 6- point
Fiery device, 7- circulation, 8- hydrogen gas tank, 9- chlorine pot, PI01- hydrogen pressure tank, PI02- chlorine pressure tank, PI03- are micro-
Mixer outlet gas pressure, PI04- microreactor outlet gas pressure, PI05- hydrogen chloride buffer tank pressure；TI01- hydrogen
Temperature, TI02- chlorine temperature, TI03- micro-mixer Outlet Gas Temperature, TIC04- microreactor Outlet Gas Temperature,
TIC05- hydrogen chloride cooler outlet pipe temp；FQIC01- hydrogen flowmeter, FQIC02- cl gas flow meter；FV01- hydrogen stream
Adjustable valve, FV02- chlorine flowrate regulating valve, TV01- circulating hot water regulating valve, TV02- hydrogen chloride cooler recirculated water are adjusted
Valve；CICR01- on-line checking point.
Specific embodiment
Present invention will be further explained below with reference to the attached drawings and examples.
As shown in Figure 1, of the invention is used to produce micro- reaction system of hydrogen chloride, including it is sequentially connected by process pipe
Micro-mixer 1, microreactor 2, hydrogen chloride cooler 3, hydrogen chloride buffer tank 4；It further include hot water cyclesystem 5, igniting dress
Set 6, circulation 7, hydrogen gas tank 8 and chlorine pot 9；The hydrogen gas tank 8, chlorine pot 9 are connect with micro-mixer 1, the igniting
Device 6, hot water cyclesystem 5 are connect with microreactor 2, and the circulation 7 is connect with hydrogen chloride cooler 4；It is described micro-
Reactor 2 is set including air-tight chamber 201 and the reaction zone 202 being arranged in air-tight chamber 201, the reaction zone 202
It is equipped with several microchannels；The hot water cyclesystem 5 includes the circulation being connected to the air-tight chamber 202 of microreactor 2
Hot water upper hose 501 and circulating hot water return pipe 502；It is set respectively on the inlet duct and outlet conduit of the micro-mixer 1
It is equipped with temperature monitor and pressure sensor；On-line detector, temperature monitor are provided on 2 outlet conduit of microreactor
And pressure sensor, the on-line detector include hydrogen chloride purity detecting instrument and free chlorine contents detector；The hydrogen chloride
Surge tank 4 is provided with pressure sensor.
Embodiment one:
The production of hydrogen chloride is used for using above-mentioned apparatus according to the following steps:
(1) by Jing Guo Gan Zaochuliing hydrogen and chlorine each lead into hydrogen gas tank 8, in chlorine pot 9；Open simultaneously hydrogen and
Chlorine intake valve makes hydrogen and chlorine while entering the two entrances of micro-mixer 1, regulates and controls the molar flow ratio of hydrogen and chlorine
Hydrogen: chlorine=1.01:1.0 ratio is passed through micro-mixer 1 and is uniformly mixed, and obtains mixed gas；
(2) enter microreactor 2 from the mixed gas that micro-mixer 1 comes out, pass through 6 provocative reaction of igniter, mixing
Gas reacts in microchannel generates hydrogen chloride gas, while circulating hot water passes through the circulating hot water of hot water cyclesystem 5
Upper hose 501 enters in the air-tight chamber 201 of microreactor 2, occurs with the microchannel internal-response object of reaction zone 202
Indirect heat exchange, the circulating hot water shape by control loop hot water temperature and flow by reaction temperature control at 1900 DEG C, after heat exchange
After recycling heat generation steam by hot water cyclesystem 5 at hot water and vapor mixture, circulating hot water passes through circulating hot water and returns
Water pipe 502 returns to the heat for taking away microreactor generation, and the steam pressure is 0.5MPa；The mixed gas is being reacted
In microchannel is 10s by the time；
(3) enter hydrogen chloride cooler 3 by the hydrogen chloride gas that the reaction of microreactor 2 generates to store after circulating water
It is stored in hydrogen chloride buffer tank 4, measuring gained hydrogen chloride product purity is 98.7%.
Embodiment two:
The production of hydrogen chloride is used for using above-mentioned apparatus according to the following steps:
(1) by Jing Guo Gan Zaochuliing hydrogen and chlorine each lead into hydrogen gas tank 8, in chlorine pot 9；Open simultaneously hydrogen and
Chlorine intake valve makes hydrogen and chlorine while entering the two entrances of micro-mixer 1, regulates and controls the molar flow ratio of hydrogen and chlorine
Hydrogen: chlorine=1.03:1.0 ratio is passed through micro-mixer 1 and is uniformly mixed, and obtains mixed gas；
(2) enter microreactor 2 from the mixed gas that micro-mixer 1 comes out, pass through 6 provocative reaction of igniter, mixing
Gas reacts in microchannel generates hydrogen chloride gas, while circulating hot water passes through the circulating hot water of hot water cyclesystem 5
Upper hose 501 enters in the air-tight chamber 201 of microreactor 2, occurs with the microchannel internal-response object of reaction zone 202
Indirect heat exchange, the circulating hot water shape by control loop hot water temperature and flow by reaction temperature control at 2100 DEG C, after heat exchange
After recycling heat generation steam by hot water cyclesystem 5 at hot water and vapor mixture, circulating hot water passes through circulating hot water and returns
Water pipe 502 returns to the heat for taking away microreactor generation, and the steam pressure is 1.1MPa；The mixed gas is being reacted
In microchannel is 12s by the time；
(3) enter hydrogen chloride cooler 3 by the hydrogen chloride gas that the reaction of microreactor 2 generates to store after circulating water
It is stored in hydrogen chloride buffer tank 4, measuring gained hydrogen chloride product purity is 98.5%.
Embodiment three:
The production of hydrogen chloride is used for using above-mentioned apparatus according to the following steps:
(1) by Jing Guo Gan Zaochuliing hydrogen and chlorine each lead into hydrogen gas tank 8, in chlorine pot 9；Open simultaneously hydrogen and
Chlorine intake valve makes hydrogen and chlorine while entering the two entrances of micro-mixer 1, regulates and controls the molar flow ratio of hydrogen and chlorine
Hydrogen: chlorine=1.05:1.0 ratio is passed through micro-mixer 1 and is uniformly mixed, and obtains mixed gas；
(2) enter microreactor 2 from the mixed gas that micro-mixer 1 comes out, pass through 6 provocative reaction of igniter, mixing
Gas reacts in microchannel generates hydrogen chloride gas, while circulating hot water passes through the circulating hot water of hot water cyclesystem 5
Upper hose 501 enters in the air-tight chamber 201 of microreactor 2, occurs with the microchannel internal-response object of reaction zone 202
Indirect heat exchange, the circulating hot water shape by control loop hot water temperature and flow by reaction temperature control at 2100 DEG C, after heat exchange
After recycling heat generation steam by hot water cyclesystem 5 at hot water and vapor mixture, circulating hot water passes through circulating hot water and returns
Water pipe 502 returns to the heat for taking away microreactor generation, and the steam pressure is 1.9MPa；The mixed gas is being reacted
In microchannel is 18s by the time；
(3) enter hydrogen chloride cooler 3 by the hydrogen chloride gas that the reaction of microreactor 2 generates to store after circulating water
It is stored in hydrogen chloride buffer tank 4, measuring gained hydrogen chloride product purity is 98.1%.
The above, only of the invention enumerates preferable example, does not make in any form and substantially to the present invention
Limitation, it is noted that for those skilled in the art, under the premise of not departing from the method for the present invention, can also do
Numerous improvement and supplement out, these are improved and supplement should also be as being considered as protection scope of the present invention.It is all not depart from the present invention
Spirit and scope in the case where, when using invent revealed content above and variation, modification and the differentiation made etc.
It is equivalent embodiment of the invention with variation；Meanwhile all substantial technologicals according to the present invention are appointed to made by above-described embodiment
Variation, modification and the differentiation of what equivalent variations, should all belong to the technical scheme of the invention.
Claims (6)
1. micro- reaction system for producing hydrogen chloride, it is characterised in that: including microreactor (2), synthetic reaction is in micro- reaction
It is carried out in device (2).
2. according to claim 1 for producing micro- reaction system of hydrogen chloride, it is characterised in that: described for producing chlorine
The micro- reaction system for changing hydrogen includes by the sequentially connected micro-mixer of process pipe (1), microreactor (2), and hydrogen chloride is cooling
Device (3), hydrogen chloride buffer tank (4)；It further include the igniter (6) for provocative reaction.
3. according to claim 2 for producing micro- reaction system of hydrogen chloride, it is characterised in that: the microreactor
(2) reaction zone (202) for including air-tight chamber (201) and being arranged in air-tight chamber (201), the reaction zone
(202) it is provided at least one microchannel.
4. according to claim 3 for producing micro- reaction system of hydrogen chloride, it is characterised in that: described for producing chlorine
The micro- reaction system for changing hydrogen further includes hot water cyclesystem (5), and the hot water cyclesystem (5) includes and microreactor (2)
The circulating hot water upper hose (501) and circulating hot water return pipe (502) of air-tight chamber (201) connection.
5. for producing micro- reaction system of hydrogen chloride according to any claim in claim 2~4, feature exists
In: temperature monitor and pressure sensor are respectively arranged on the inlet duct and outlet conduit of the micro-mixer (1)；Institute
It states and is provided with on-line detector, temperature monitor and pressure sensor, the on-line detector on microreactor (2) outlet conduit
Including hydrogen chloride purity detecting instrument and free chlorine contents detector；The hydrogen chloride buffer tank (4) is provided with pressure sensor.
6. utilizing the method for micro- reaction system production hydrogen chloride, comprising the following steps:
A, by dry hydrogen and chlorine according to the molar ratio hydrogen of flows per unit time: chlorine=1.01~1.05:1 ratio
It is passed through in micro-mixer (1) and is sufficiently mixed simultaneously, obtain mixed gas；
B, enter microreactor (2) from the mixed gas that micro-mixer (1) comes out, pass through igniter (6) provocative reaction, mixing
Gas reacts in microchannel generates hydrogen chloride gas, while circulating hot water passes through the cycling hot of hot water cyclesystem (5)
Water pipe (501) waterborne enters in the air-tight chamber (201) of microreactor (2), inside the microchannel of reaction zone (202)
Indirect heat exchange occurs for reactant, and reaction temperature is controlled at 1500~2500 DEG C；The mixed gas is in microchannel
It is 5~20s by the time；
C, the hydrogen chloride gas that reaction generates obtains chlorination hydrogen production after cooling.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811404363.6A CN109336052A (en) | 2018-11-23 | 2018-11-23 | For producing micro- reaction system of hydrogen chloride and the hydrogen chloride production method based on the system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811404363.6A CN109336052A (en) | 2018-11-23 | 2018-11-23 | For producing micro- reaction system of hydrogen chloride and the hydrogen chloride production method based on the system |
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| Publication Number | Publication Date |
|---|---|
| CN109336052A true CN109336052A (en) | 2019-02-15 |
Family
ID=65317327
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811404363.6A Pending CN109336052A (en) | 2018-11-23 | 2018-11-23 | For producing micro- reaction system of hydrogen chloride and the hydrogen chloride production method based on the system |
Country Status (1)
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1186042A (en) * | 1997-12-20 | 1998-07-01 | 巴陵石化岳阳石油化工总厂 | Method and apparatus for producing high purity hydrochloric acid from chlorine tailings as by product from liquefaction of dry chlorine gas |
| US20040191707A1 (en) * | 2003-03-31 | 2004-09-30 | Tetsurou Mitsui | Emulsion of silver halide fine grains and process for the preparation of emulsion of silver halide tabular grains |
| CN1640813A (en) * | 2004-01-15 | 2005-07-20 | 山东滨化集团有限责任公司 | Method for producing reagent-level hydrochloric acid |
| CN101448736A (en) * | 2006-05-23 | 2009-06-03 | 拜尔材料科学股份公司 | Process for the oxidation of hydrogen chloride-containing gas |
| US20110168210A1 (en) * | 2007-10-24 | 2011-07-14 | Fuji Xerox Co., Ltd. | Micro-nano bubble generating method, microchannel cleaning method, micro-nano bubble generating system, and microreactor |
| CN103221336A (en) * | 2011-10-11 | 2013-07-24 | 宏仁化学株式会社 | Method and system for preparing high-purity hydrogen chloride |
| CN108129384A (en) * | 2018-02-01 | 2018-06-08 | 黑龙江禾馗农业科技有限公司 | N-serve method for production of phosphate salt |
-
2018
- 2018-11-23 CN CN201811404363.6A patent/CN109336052A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1186042A (en) * | 1997-12-20 | 1998-07-01 | 巴陵石化岳阳石油化工总厂 | Method and apparatus for producing high purity hydrochloric acid from chlorine tailings as by product from liquefaction of dry chlorine gas |
| US20040191707A1 (en) * | 2003-03-31 | 2004-09-30 | Tetsurou Mitsui | Emulsion of silver halide fine grains and process for the preparation of emulsion of silver halide tabular grains |
| CN1640813A (en) * | 2004-01-15 | 2005-07-20 | 山东滨化集团有限责任公司 | Method for producing reagent-level hydrochloric acid |
| CN101448736A (en) * | 2006-05-23 | 2009-06-03 | 拜尔材料科学股份公司 | Process for the oxidation of hydrogen chloride-containing gas |
| US20110168210A1 (en) * | 2007-10-24 | 2011-07-14 | Fuji Xerox Co., Ltd. | Micro-nano bubble generating method, microchannel cleaning method, micro-nano bubble generating system, and microreactor |
| CN103221336A (en) * | 2011-10-11 | 2013-07-24 | 宏仁化学株式会社 | Method and system for preparing high-purity hydrogen chloride |
| CN108129384A (en) * | 2018-02-01 | 2018-06-08 | 黑龙江禾馗农业科技有限公司 | N-serve method for production of phosphate salt |
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| Title |
|---|
| S. MAEHARA ET AL.: "Catalytic synthesis of hydrogen peroxide in microreactors", vol. 86, no. 4, pages 410 - 415, XP022574786 * |
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