CN109956452A - A kind of preparation method and its device of reagent hydrochloric acid - Google Patents
A kind of preparation method and its device of reagent hydrochloric acid Download PDFInfo
- Publication number
- CN109956452A CN109956452A CN201910296434.3A CN201910296434A CN109956452A CN 109956452 A CN109956452 A CN 109956452A CN 201910296434 A CN201910296434 A CN 201910296434A CN 109956452 A CN109956452 A CN 109956452A
- Authority
- CN
- China
- Prior art keywords
- hydrochloric acid
- film
- grades
- hydrogen chloride
- tower
- 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.)
- Granted
Links
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 163
- 239000003153 chemical reaction reagent Substances 0.000 title claims abstract description 42
- 238000002360 preparation method Methods 0.000 title claims abstract description 24
- 238000010521 absorption reaction Methods 0.000 claims abstract description 69
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 50
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 50
- 239000007789 gas Substances 0.000 claims abstract description 49
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000000460 chlorine Substances 0.000 claims abstract description 29
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000001257 hydrogen Substances 0.000 claims abstract description 21
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 21
- 238000000034 method Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 229910021642 ultra pure water Inorganic materials 0.000 claims abstract description 7
- 239000012498 ultrapure water Substances 0.000 claims abstract description 7
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 230000009102 absorption Effects 0.000 claims description 64
- 239000002253 acid Substances 0.000 claims description 9
- 238000009826 distribution Methods 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 2
- 238000001354 calcination Methods 0.000 claims description 2
- 229910002804 graphite Inorganic materials 0.000 claims description 2
- 239000010439 graphite Substances 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 11
- 239000006096 absorbing agent Substances 0.000 abstract description 6
- 239000002994 raw material Substances 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 4
- 239000002912 waste gas Substances 0.000 abstract description 3
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 abstract 1
- 230000000052 comparative effect Effects 0.000 description 7
- 239000012535 impurity Substances 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 239000002699 waste material Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 230000007547 defect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000011031 large-scale manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000002163 immunogen Effects 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000012372 quality testing Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 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 preparation method of reagent hydrochloric acid and its devices, chlorine and hydrogen are sent into graphitic synthetic furnace, the hydrogen chloride gas of synthesis is sent into hydrogen chloride cooler and is cooled down, hydrogen chloride gas after cooling enters I grades of film-falling absorption towers, it is absorbed in tower by the dilute hydrochloric acid from II grades of film-falling absorption towers and generates reagent grade hydrochloric acid, the hydrogen chloride gas that I grades of film-falling absorption towers come out enters II grades of film-falling absorption towers, it is absorbed in tower by ultrapure water and generates dilute hydrochloric acid, the hydrogen chloride gas come out from II grades of film-falling absorption towers enters tail gas absorber, dilute hydrochloric acid is generated by absorbing pure water in tower and is recycled.This method simple production process, with low investment, occupied area is small, produces high-efficient, and raw material availability is high, and product quality is high, and energy consumption is low, and production cost is low, no waste water and gas discharge, and easy to repair, control is easy to operate, it can be achieved that continuous-stable is mass produced.
Description
Technical field
The invention belongs to chemical production fields, and in particular to a kind of preparation method and its device of reagent hydrochloric acid.
Background technique
In the prior art, there are two types of the production methods of reagent grade hydrochloric acid, including one-step method and two-step method.One step technique side
Case: by chlorine and hydrogen in synthetic furnace synthesizing chlorinated hydrogen, carry out after cooling removal of impurities reaction (using it is one or more also
Immunogenic substance is reacted with the impurity in hydrogen chloride gas), the hydrogen chloride gas after removal of impurities is absorbed through three-level absorption plant to be made
Reagent hydrochloric acid is obtained, unabsorbed tail gas is absorbed as dilute hydrochloric acid through hydraulic jet pump.Its major defect is: the liquid after removal of impurities
Environment is polluted, processing difficulty is big；Absorb long flow path, unstable product quality；Hydrogen chloride utilization rate is low, and diluted acid amount is big.
Two-step mode technique scheme: the first step synthesizing chlorinated hydrogen in synthetic furnace by chlorine and hydrogen is used after cooling
Absorbing pure water hydrogen chloride gas produces common hydrochloric acid；Second step, which evaporates common hydrochloric acid by reboiler, produces purer hydrogen chloride
Gas, then reagent grade hydrochloric acid is produced with absorbing pure water hydrogen chloride gas.Its major defect is: process is complicated, and control point is more；
Equipment therefor is more, takes up a large area, high investment；The utilization rate of the low efficiency produced, hydrogen chloride gas is relatively low, there is one
Divide hydrogen chloride gas that can not separate, raw material availability is low；Operate large labor intensity；Maintenance work difficulty is big, and risk is higher；It needs
It consumes a large amount of heat of vaporization hydrochloric acid and produces purer hydrogen chloride gas, consume energy larger；The hydrogen chloride gas evaporated holds
Environmental pollution is easily caused, absorption can also generate acid waste water, will cause certain harm to environment；Without continuous extensive raw
The ability of production.
In view of above-mentioned deficiency, a kind of simple production process, with low investment, occupied area is small, produces high-efficient, raw material availability
Height, product quality is high, and energy consumption is low, and production cost is low, and no waste water and gas discharge, easy to repair, control is easy to operate, can
The reagent hydrochloric acid device for realizing continuous-stable large-scale production is badly in need of in current industry.
Summary of the invention
Based on above-mentioned analysis, the present invention provides a kind of production method of reagent grade hydrochloric acid, to simplify production technology, improves system
Efficiency is taken, plant investment is reduced, realizes energy-saving, zero environmental and continuous-stable large-scale production.The present invention is to pass through
What following scheme was realized:
A kind of device of reagent preparation hydrochloric acid, the device by Chlorine Buffer Vessel (1), hydrogen gas buffer (2), graphitic synthetic furnace (3),
Cooler (4), distribution platform (5), I grades of film-falling absorption towers (6), II grades of film-falling absorption towers (7), tail gas absorber (8), dilute acid bath
(9), diluted acid force (forcing) pump (10), reagent hydrochloric acid storage tank (11) composition.
A kind of preparation method of reagent hydrochloric acid, this method comprises the following steps:
(I) prepares chlorine and enters in graphitic synthetic furnace (3) through Chlorine Buffer Vessel (1), and hydrogen enters graphite through hydrogen gas buffer (2)
In synthetic furnace (3), two kinds of gases generate hydrogen chloride gas under burning condition, after hydrogen chloride cooler (4) carries out cooling, then
Platform (5) are distributed into hydrogen chloride, enter back into I grades of film-falling absorption towers (6), the dilute of II grades of film-falling absorption towers (7) is come from tower
Absorption by Hydrochloric Acid generates reagent grade hydrochloric acid, and reagent grade hydrochloric acid flows into reagent grade hydrochloric acid tank (11) from I grades of film-falling absorption tower (6) tower bottom；
The hydrogen chloride gas that (II) comes out through I grades of film-falling absorption towers (6) enters II grades of film-falling absorption towers (7), ultrapure in tower
Water absorb generate 10 ~ 20%(wt) dilute hydrochloric acid, from II grade film-falling absorption towers (7) out hydrogen chloride gas enter tail gas absorption
Tower (8) generates dilute hydrochloric acid by absorbing pure water in tower, and unabsorbed tail gas is from II grades of film-falling absorption tower top discharges.
Further, the purity of chlorine gas feeding is 98.5 ~ 98.8%, oxygen content≤0.3%, flow 200Nm3/h.
Further, the hydrogen purity is 99.8 ~ 99.9%, and flow is 215 Nm3/h.
Further, the hydrogen chloride is cooled to 40 DEG C or less.
Further, the graphitic synthetic furnace outlet pressure control is in 15 ~ 50kPa.
Further, the hydrogen chloride flow from distribution platform is 420 ~ 425Nm3/h, and purity is 94.5 ~ 95.3%, trip
From chlorinity < 0.2ppm.
Further, 35 DEG C of the dilute hydrochloric acid temperature < of the II grades of film-falling absorption tower, concentration 6 ~ 20%.
Further, the reagent grade hydrochloric acid concentration is 36 ~ 38%.
Further, the resistivity of the ultrapure water >=15M Ω, ignition residue≤0.0001 %.
Further, the film-falling absorption tower material uses the special impregnation technology of proprietary formula modified resin, is patrolled three times
The heat treatment returned under high temperature, high pressure makes resin impregnated, carbonization.
Further, the synthetic furnace combustion system careful design hydrogen and chlorine aisle spare control hydrogen, cl gas flow
The optimal proportion of speed, enables chlorine and hydrogen to be come into full contact with, be burnt, and improves HCL quality.
The beneficial effects of the present invention are:
1, it is 32 ~ 33(mass ratio by accurately control chlorine/hydrogen flowing quantity ratio), accurately control chlorine/hydrogen flow rate ratio
1.49-1.51 accurately controls chlorine/Hydrogen Vapor Pressure (0.12/0.08MPa)；With ultrapure water quality, (calcination is residual for strict control absorption
Slag≤0.0001%, resistivity >=15M Ω) and hydrogen chloride gas impurity；Strict control hydrogen chloride gas and absorption water flow (chlorine
Change hydrogen and absorption water flow ratio are 0.575-0.590) and system pressure (hydrogen chloride gas pressure and absorption water flow pressure
Power is respectively 0.01MPa and 0.32MPa, and system pressure is controlled in 0.008-0.015MPa), finally realize simple production process,
With low investment, occupied area is small, produces high-efficient, and raw material availability is high, and product quality is high, and energy consumption is low, and production cost is low, nothing
Waste water and gas discharge, easy to repair, control are easy to operate, it can be achieved that the reagent hydrochloric acid device that continuous-stable is mass produced.
2, compared with existing one-step method, exclusion device and impurity removal process are saved, reduces discharging of waste liquid, reduces material consumption energy consumption；
Absorption process is short, and device is few, and absorption efficiency is high, and diluted acid amount is few, and product quality is high.
3, compared with two-step method, process is simple, and device is few, with low investment, high-efficient, easy to operate, safety and environmental protection, raw material benefit
With rate height, production cost is low, can continuously be mass produced.
Detailed description of the invention
Fig. 1 is apparatus of the present invention figure, wherein 1 is Chlorine Buffer Vessel, 2 be hydrogen gas buffer, and 3 be graphitic synthetic furnace, and 4 be cold
But device, 5 be distribution platform, and 6 be I grade of film-falling absorption tower, and 7 be II grade of film-falling absorption tower, and 8 be tail gas absorber, and 9 be dilute acid bath, 10
It is reagent hydrochloric acid storage tank for diluted acid force (forcing) pump, 11.
Specific embodiment
Embodiment 1
A kind of preparation method of reagent hydrochloric acid
Purity is 98.6%(volume ratio), oxygen content 0.3%, flow is the chlorine of 200Nm3/h after Chlorine Buffer Vessel (1)
Into in graphitic synthetic furnace, purity is 99.8%(volume ratio), flow is that the hydrogen of 215Nm3/h is laggard through hydrogen gas buffer (2)
Enter in graphitic synthetic furnace (3).Into synthetic furnace chlorine and hydrogen in furnace combustion reaction generate hydrogen chloride gas, through hydrogen chloride
Cooler (4) is cooled to 40 DEG C hereinafter, distributing platform (5) into hydrogen chloride, and graphitic synthetic furnace outlet pressure is controlled in 33kPa.Come
Enter I grades of drops from the hydrogen chloride (flow 423Nm3/h, purity 94.9%, free chlorine contents are less than 0.2ppm) of distribution platform (5)
Film absorption tower (6), by dilute hydrochloric acid (temperature less than 35 DEG C, the concentration 23%) absorption from II grade film-falling absorption towers (7) in tower
It generates reagent grade hydrochloric acid (37%), reagent grade hydrochloric acid flows into reagent grade hydrochloric acid tank (11) from I grades of film-falling absorption tower tower bottom.
The hydrogen chloride gas (pressure 7.5kPa) that I grades of film-falling absorption towers come out enters II grades of film-falling absorption towers, in tower
It is absorbed by ultrapure water (resistivity >=15M Ω, ignition residue≤0.0001%) and generates content as the dilute hydrochloric acid of 15%(wt).From II
Grade film-falling absorption tower come out hydrogen chloride gas enter tail gas absorber (8), dilute hydrochloric acid is generated by absorbing pure water in tower, not by
(HCL content the is less than 20mg/m3) discharge up to standard at the top of absorption tower of the tail gas of absorption.
Embodiment 2
A kind of preparation method of reagent hydrochloric acid
Purity is 98.5%(volume ratio), oxygen content 0.3%, flow is the chlorine of 200Nm3/h after Chlorine Buffer Vessel (1)
Into in graphitic synthetic furnace, purity is 99.8%(volume ratio), flow is that the hydrogen of 215Nm3/h is laggard through hydrogen gas buffer (2)
Enter in graphitic synthetic furnace (3).Into synthetic furnace chlorine and hydrogen in furnace combustion reaction generate hydrogen chloride gas, through hydrogen chloride
Cooler (4) is cooled to 40 DEG C hereinafter, distributing platform (5) into hydrogen chloride, and graphitic synthetic furnace outlet pressure is controlled in 15kPa.Come
Enter I grades of drops from the hydrogen chloride (flow 420Nm3/h, purity 94.5%, free chlorine contents are less than 0.2ppm) of distribution platform (5)
Film absorption tower (6), by dilute hydrochloric acid (temperature less than 35 DEG C, the concentration 15%) absorption from II grade film-falling absorption towers (7) in tower
It generates reagent grade hydrochloric acid (36%), reagent grade hydrochloric acid flows into reagent grade hydrochloric acid tank (11) from I grades of film-falling absorption tower tower bottom.
The hydrogen chloride gas (pressure 5kPa) that I grades of film-falling absorption towers come out enters II grades of film-falling absorption towers, the quilt in tower
Ultrapure water (resistivity >=15M Ω, ignition residue≤0.0001 %), which absorbs, generates content as the dilute hydrochloric acid of 10%(wt).From II grades
The hydrogen chloride gas that film-falling absorption tower comes out enters tail gas absorber (8), generates dilute hydrochloric acid by absorbing pure water in tower, is not inhaled
(HCL content the is less than 20mg/m3) discharge up to standard at the top of absorption tower of the tail gas of receipts.
Embodiment 3
A kind of preparation method of reagent hydrochloric acid
Purity is 98.8%(volume ratio), oxygen content 0.3%, flow is the chlorine of 200Nm3/h after Chlorine Buffer Vessel (1)
Into in graphitic synthetic furnace, purity is 99.9%(volume ratio), flow is that the hydrogen of 215Nm3/h is laggard through hydrogen gas buffer (2)
Enter in graphitic synthetic furnace (3).Into synthetic furnace chlorine and hydrogen in furnace combustion reaction generate hydrogen chloride gas, through hydrogen chloride
Cooler (4) is cooled to 40 DEG C hereinafter, distributing platform (5) into hydrogen chloride, and graphitic synthetic furnace outlet pressure is controlled in 50kPa.Come
From the hydrogen chloride of distribution platform (5), (flow is 425N m3/h, and purity 95.3%, free chlorine contents are less than 0.2ppm) into I grades
Film-falling absorption tower (6), by dilute hydrochloric acid (temperature less than 35 DEG C, the concentration 30%) suction from II grade film-falling absorption towers (7) in tower
Midwifery flows into reagent grade hydrochloric acid tank (11) from I grades of film-falling absorption tower tower bottom at reagent grade hydrochloric acid (38%), reagent grade hydrochloric acid.
The hydrogen chloride gas (pressure 10kPa) that I grades of film-falling absorption towers come out enters II grades of film-falling absorption towers, the quilt in tower
Ultrapure water (resistivity >=15M Ω, ignition residue≤0.0001 %), which absorbs, generates content as the dilute hydrochloric acid of 20%(wt).From II grades
The hydrogen chloride gas that film-falling absorption tower comes out enters tail gas absorber (8), generates dilute hydrochloric acid by absorbing pure water in tower, is not inhaled
(HCL content the is less than 20mg/m3) discharge up to standard at the top of absorption tower of the tail gas of receipts.
Comparative example 1
The reagent hydrochloric acid of one-step method preparation.
Comparative example 2
The reagent hydrochloric acid of two-step method preparation.
Test example 1
The waste liquid absorption efficiency of comparative example 1, comparative example 1 and comparative example 2
Waste liquid absorption efficiency >=99.5% in 1 preparation process of embodiment, waste liquid absorption efficiency < 90% in 1 preparation process of comparative example,
Waste liquid absorption efficiency 35-40% in 2 preparation process of comparative example.
Test example 2
The quality for the reagent hydrochloric acid that embodiment 1 produces is detected, specific testing result is as shown in table 1.
The quality testing of reagent hydrochloric acid made from 1 embodiment 1 of table is reported
。
Claims (10)
1. a kind of device of reagent preparation hydrochloric acid, which is characterized in that the device by Chlorine Buffer Vessel (1), hydrogen gas buffer (2),
Graphitic synthetic furnace (3), cooler (4), distribution platform (5), I grades of film-falling absorption towers (6), II grades of film-falling absorption towers (7), tail gas absorptions
Tower (8), dilute acid bath (9), diluted acid force (forcing) pump (10), reagent hydrochloric acid storage tank (11) composition.
2. a kind of preparation method of the reagent hydrochloric acid based on claim 1 described device, which is characterized in that this method includes as follows
Step:
(I) prepares chlorine and enters in graphitic synthetic furnace (3) through Chlorine Buffer Vessel (1), and hydrogen enters graphite through hydrogen gas buffer (2)
In synthetic furnace (3), two kinds of gases generate hydrogen chloride gas under burning condition, after hydrogen chloride cooler (4) carries out cooling, then
Platform (5) are distributed into hydrogen chloride, enter back into I grades of film-falling absorption towers (6), the dilute of II grades of film-falling absorption towers (7) is come from tower
Absorption by Hydrochloric Acid generates reagent grade hydrochloric acid, and reagent grade hydrochloric acid flows into reagent grade hydrochloric acid tank (11) from I grades of film-falling absorption tower (6) tower bottom；
The hydrogen chloride gas that (II) comes out through I grades of film-falling absorption towers (6) enters II grades of film-falling absorption towers (7), ultrapure in tower
Water absorb generate 10 ~ 20%(wt) dilute hydrochloric acid, from II grade film-falling absorption towers (7) out hydrogen chloride gas enter tail gas absorption
Tower (8) generates dilute hydrochloric acid by absorbing pure water in tower, and unabsorbed tail gas is from II grades of film-falling absorption tower top discharges.
3. preparation method according to claim 2, which is characterized in that the purity of chlorine gas feeding is 98.5 ~ 98.8%, oxygen content
≤ 0.3%, flow 200Nm3/h.
4. preparation method according to claim 2, which is characterized in that the hydrogen purity is 99.8 ~ 99.9%, and flow is
215 Nm³/h。
5. preparation method according to claim 2, which is characterized in that the hydrogen chloride is cooled to 40 DEG C or less.
6. preparation method according to claim 2, which is characterized in that graphitic synthetic furnace outlet pressure control 15 ~
50kPa。
7. preparation method according to claim 2, which is characterized in that it is described from distribution platform hydrogen chloride flow be 420 ~
425Nm3/h, purity are 94.8 ~ 95.3%, free chlorine contents < 0.2ppm.
8. preparation method according to claim 2, which is characterized in that the dilute hydrochloric acid temperature < of the II grades of film-falling absorption tower
35 DEG C, concentration 6 ~ 20%.
9. preparation method according to claim 2, which is characterized in that the reagent grade hydrochloric acid concentration is 36 ~ 38%.
10. preparation method according to claim 2, which is characterized in that the resistivity of the ultrapure water >=15M Ω, calcination
Residue≤0.0001 %.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910296434.3A CN109956452B (en) | 2019-04-13 | 2019-04-13 | Preparation method and device of reagent hydrochloric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910296434.3A CN109956452B (en) | 2019-04-13 | 2019-04-13 | Preparation method and device of reagent hydrochloric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109956452A true CN109956452A (en) | 2019-07-02 |
| CN109956452B CN109956452B (en) | 2022-07-29 |
Family
ID=67026153
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910296434.3A Active CN109956452B (en) | 2019-04-13 | 2019-04-13 | Preparation method and device of reagent hydrochloric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109956452B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112028737A (en) * | 2020-09-14 | 2020-12-04 | 河南神马氯碱发展有限责任公司 | Method and device for preparing chloroethylene by treating bis (trichloromethyl) carbonate production tail gas through combustion method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2679132Y (en) * | 2004-01-15 | 2005-02-16 | 山东滨化集团有限责任公司 | Prodn. appts. for reagent-class hydrochloric acid |
| CN1587027A (en) * | 2004-08-30 | 2005-03-02 | 金川集团有限公司 | Method for producing reagent hydrochloric acid |
| 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 |
| EP1671926A1 (en) * | 2004-12-15 | 2006-06-21 | Sgl Carbon Ag | Method for utilizing the cooling water of hydrogen chloride synthesis plants |
| CN104150443A (en) * | 2014-07-31 | 2014-11-19 | 河南永银化工实业有限公司 | High-concentration hydrochloric acid production device |
| WO2017026259A1 (en) * | 2015-08-10 | 2017-02-16 | 昭和電工株式会社 | Method for producing hydrogen chloride |
| CN108313982A (en) * | 2018-04-20 | 2018-07-24 | 江苏安邦电化有限公司 | A kind of device that dilute hydrochloric acid enrichment decolourizes and the method for preparing decoloration hydrochloric acid |
-
2019
- 2019-04-13 CN CN201910296434.3A patent/CN109956452B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2679132Y (en) * | 2004-01-15 | 2005-02-16 | 山东滨化集团有限责任公司 | Prodn. appts. for reagent-class hydrochloric acid |
| 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 |
| CN1587027A (en) * | 2004-08-30 | 2005-03-02 | 金川集团有限公司 | Method for producing reagent hydrochloric acid |
| EP1671926A1 (en) * | 2004-12-15 | 2006-06-21 | Sgl Carbon Ag | Method for utilizing the cooling water of hydrogen chloride synthesis plants |
| CN104150443A (en) * | 2014-07-31 | 2014-11-19 | 河南永银化工实业有限公司 | High-concentration hydrochloric acid production device |
| WO2017026259A1 (en) * | 2015-08-10 | 2017-02-16 | 昭和電工株式会社 | Method for producing hydrogen chloride |
| CN108313982A (en) * | 2018-04-20 | 2018-07-24 | 江苏安邦电化有限公司 | A kind of device that dilute hydrochloric acid enrichment decolourizes and the method for preparing decoloration hydrochloric acid |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112028737A (en) * | 2020-09-14 | 2020-12-04 | 河南神马氯碱发展有限责任公司 | Method and device for preparing chloroethylene by treating bis (trichloromethyl) carbonate production tail gas through combustion method |
| CN112028737B (en) * | 2020-09-14 | 2023-03-31 | 河南神马氯碱发展有限责任公司 | Method and device for preparing chloroethylene by treating bis (trichloromethyl) carbonate production tail gas through combustion method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109956452B (en) | 2022-07-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8287830B2 (en) | Devices for preparing ammonium bicarbonate with flue gas and method of using the devices | |
| CN101235160B (en) | Hydrogen chloride whole reclaiming zero discharging technique and device for PVC producing process | |
| CN1615270A (en) | Aqueous borohydride compositions | |
| CN111039267B (en) | Device and method for prepurifying electrolytic prepared nitrogen trifluoride crude product | |
| CN106139890A (en) | Cold-rolled steel sheet heat treatment nitrogen hydrogen mixed tail gas reclaims the apparatus and method purifying | |
| CN108557766B (en) | Refining method of hydrogen chloride | |
| CN111533091A (en) | Production device and production process of EL-grade sulfuric acid | |
| US8506925B1 (en) | Iodine-sulfur cycle for nuclear hydrogen production with improved thermo-chemical efficiency | |
| CN106477525B (en) | Method for purifying chlorination tail gas chlorine hydride dechlorination gas | |
| CN111675195A (en) | Energy-saving environment-friendly process flow for synthesizing hydrochloric acid | |
| CN106007087B (en) | A kind of high-concentration ammonia nitrogenous wastewater treatment process and ammonia recovery system | |
| CN109956452A (en) | A kind of preparation method and its device of reagent hydrochloric acid | |
| CN105695655A (en) | System and method for preparing clean gas base vertical furnace reducing gas through coal gasification | |
| CN210103457U (en) | Device for preparing and producing high-purity sulfur dioxide by utilizing acid gas | |
| CN105000745B (en) | A kind of sulfur Gas Fields produced water treatment system | |
| CN106044710A (en) | Method for purifying electron-grade hydrogen chloride | |
| CN101016159A (en) | Method of synthesizing ammonia by hydrogen gas purified by tail gas of sodium cyanide and alkali-chloride production | |
| CN104318968A (en) | Process and device for treating tritium-containing water in nuclear power plant based on electrolysis and low-temperature distillation cascade process | |
| CN103030117B (en) | Recovering technology for waste acid | |
| CN207986685U (en) | hydrogen peroxide oxidation tower | |
| CN102351149A (en) | System for recovering and removing chlorine from hydrogen chloride | |
| CN113509811A (en) | Method and system for treating tail gas containing chloropropene and oxygen | |
| CN105776696A (en) | Process for concentrating waste liquor from caprolactam production | |
| CN205635670U (en) | System for clean gas of coal gasification preparation base shaft furnace is crude gas still | |
| CN106139823B (en) | A kind of comprehensive reutilization method of coal chemical industry transformation condensate liquid stripping tail gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 611930 No.166 Linyang Road, Jiuchi Town, Pengzhou City, Chengdu City, Sichuan Province Applicant after: Huarong Chemical Co.,Ltd. Address before: 611930 No.166 Linyang Road, Jiuchi Town, Pengzhou City, Chengdu City, Sichuan Province Applicant before: CHENGDU HUARONG CHEMICAL Co.,Ltd. |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20230918 Address after: 611930 No.166 Linyang Road, Jiuchi Town, Pengzhou City, Chengdu City, Sichuan Province Patentee after: Huarong Chemical (Chengdu) Co.,Ltd. Address before: 611930 No.166 Linyang Road, Jiuchi Town, Pengzhou City, Chengdu City, Sichuan Province Patentee before: Huarong Chemical Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20231206 Address after: 611930 No.166 Linyang Road, Jiuchi Town, Pengzhou City, Chengdu City, Sichuan Province Patentee after: Huarong Chemical Co.,Ltd. Patentee after: Huarong Chemical (Chengdu) Co.,Ltd. Address before: 611930 No.166 Linyang Road, Jiuchi Town, Pengzhou City, Chengdu City, Sichuan Province Patentee before: Huarong Chemical (Chengdu) Co.,Ltd. |
|
| TR01 | Transfer of patent right |