CN114588650B - Combined hydrochloric acid resolving process - Google Patents
Combined hydrochloric acid resolving process Download PDFInfo
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- CN114588650B CN114588650B CN202210232327.6A CN202210232327A CN114588650B CN 114588650 B CN114588650 B CN 114588650B CN 202210232327 A CN202210232327 A CN 202210232327A CN 114588650 B CN114588650 B CN 114588650B
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- hydrochloric acid
- tower
- dehydration concentration
- calcium chloride
- extraction
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- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 370
- 238000000034 method Methods 0.000 title claims abstract description 39
- 230000018044 dehydration Effects 0.000 claims abstract description 58
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 58
- 238000004458 analytical method Methods 0.000 claims abstract description 39
- 238000004821 distillation Methods 0.000 claims abstract description 38
- 238000000605 extraction Methods 0.000 claims abstract description 38
- 239000002253 acid Substances 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 31
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 38
- 239000007789 gas Substances 0.000 claims description 35
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 28
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 28
- 239000001110 calcium chloride Substances 0.000 claims description 25
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 25
- 239000002699 waste material Substances 0.000 claims description 15
- 238000009835 boiling Methods 0.000 claims description 9
- 239000003595 mist Substances 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 6
- 230000008020 evaporation Effects 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 3
- 230000002378 acidificating effect Effects 0.000 claims description 2
- 125000004122 cyclic group Chemical group 0.000 claims description 2
- 239000002994 raw material Substances 0.000 claims description 2
- 230000006837 decompression Effects 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 238000005516 engineering process Methods 0.000 abstract description 3
- 238000003795 desorption Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-DYCDLGHISA-N deuterium hydrogen oxide Chemical compound [2H]O XLYOFNOQVPJJNP-DYCDLGHISA-N 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- DKAGJZJALZXOOV-UHFFFAOYSA-N hydrate;hydrochloride Chemical compound O.Cl DKAGJZJALZXOOV-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/40—Extractive distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
-
- 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
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0712—Purification ; Separation of hydrogen chloride by distillation
-
- 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
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0731—Purification ; Separation of hydrogen chloride by extraction
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to the technical field of hydrochloric acid analysis, and particularly discloses a combined hydrochloric acid analysis process, which is characterized in that high enthalpy acid-containing water vapor generated in the hydrochloric acid extraction and distillation process is used for supplying heat to a reboiler of a hydrochloric acid dehydration concentration tower in a hydrochloric acid pressure swing distillation method, and a large amount of enthalpy taken away by the acid-containing water vapor in the extraction and distillation method in the hydrochloric acid analysis process technology is recycled to the hydrochloric acid dehydration concentration tower in the hydrochloric acid pressure swing distillation process, so that the energy consumption of the hydrochloric acid analysis process is reduced by more than 25%.
Description
Technical Field
The invention relates to the technical field of hydrochloric acid analysis, in particular to a combined hydrochloric acid analysis process.
Background
The hydrochloric acid resolving process used in the industry at present comprises an extraction and distillation method, a differential pressure resolving method and a conventional desorption method, wherein the extraction and distillation method is low in direct energy consumption and mature in process, but equipment is blocked due to enrichment of hydrochloric acid impurities in the operation process, so that the overhaul cost is high; the differential pressure analysis method can use a filtering device to filter and remove impurities from the circulating materials, but has higher energy consumption; the conventional desorption method has low energy consumption, the concentration of the generated waste acid water is generally about 18%, the waste acid water is difficult to treat due to higher concentration, and in the current process for generating waste acid water and hydrogen chloride with the concentration of less than 1% by hydrochloric acid analysis, the energy consumption for treating each ton of hydrochloric acid is at least 1.6t, and the energy consumption is larger, so that the combined hydrochloric acid analysis process with lower energy consumption is provided.
Disclosure of Invention
The invention aims to provide a combined hydrochloric acid analysis process for solving the problems in the background technology.
In order to achieve the above purpose, the present invention provides the following technical solutions: a combined hydrochloric acid resolving process comprises the following steps:
step 1: resolving hydrochloric acid in a hydrochloric acid extraction and distillation tower by taking a calcium chloride solution as an extractant, wherein gas at the top of the extraction and distillation tower is condensed by a condenser at the top of the extraction and distillation tower and then is subjected to mist removal by a hydrogen chloride gas demister of the extraction and distillation tower to generate hydrogen chloride gas, dilute calcium chloride extracted from a tower kettle enters a calcium chloride flash tank and a calcium chloride flash reboiler for heating, and normal-pressure acidic water vapor and a calcium chloride solution are generated after the calcium chloride flash tank is depressurized to micro-positive pressure flash evaporation, and the calcium chloride solution is recycled by a calcium chloride circulating pump and enters the hydrochloric acid extraction and distillation tower for recycling;
step 2: extracting hydrochloric acid in a hydrochloric acid analysis tower, condensing tower top gas through a condenser at the top of the hydrochloric acid analysis tower, removing mist through a hydrogen chloride gas demister of the hydrochloric acid analysis tower to generate hydrogen chloride gas, extracting constant boiling acid from a tower bottom to enter a hydrochloric acid dehydration concentration tower in a negative pressure state, condensing acid-containing water vapor produced at the top of the hydrochloric acid dehydration concentration tower through the condenser at the top of the hydrochloric acid dehydration concentration tower, and then entering a waste acid tank of the hydrochloric acid dehydration concentration tower, wherein concentrated hydrochloric acid extracted from the tower bottom enters hydrochloric acid in the hydrochloric acid analysis tower again through a hydrochloric acid dehydration concentration conveying pump for cyclic analysis;
step 3: the water vapor reboiler of the hydrochloric acid dehydration concentration tower for providing a heating function for the hydrochloric acid dehydration concentration tower is heated by generating normal-pressure acid water vapor after the pressure in the calcium chloride flash tank is reduced to micro-positive pressure flash evaporation in the step 1.
Preferably, in the step 1, the purity of the hydrogen chloride gas generated by condensing the gas at the top of the hydrochloric acid extraction distillation column through a condenser at the top of the extraction distillation column and removing mist through a hydrogen chloride gas demister of the extraction distillation column is 99.99%; in the step 2, hydrochloric acid is extracted in a hydrochloric acid analysis tower, wherein the purity of the gas at the top of the hydrochloric acid analysis tower is 99.99% after the gas at the top of the hydrochloric acid analysis tower is condensed by a condenser at the top of the hydrochloric acid analysis tower and mist is removed by a hydrogen chloride gas demister of the hydrochloric acid analysis tower.
Preferably, in the step 1, the temperature of the extracting agent calcium chloride solution is 133 ℃, and the concentration of the extracting agent calcium chloride solution is 50% -60%.
Preferably, in step 2, the concentration of the raw material hydrochloric acid entering the hydrochloric acid analysis tower is at least 23%.
Preferably, in the step 2, constant boiling acid extracted from the bottom of the hydrochloric acid resolving tower is kept constant boiling by a reboiler of the hydrochloric acid resolving tower and then enters a hydrochloric acid dehydration concentration tower in a negative pressure state.
Preferably, in the step 2, concentrated hydrochloric acid extracted from the tower bottom of the hydrochloric acid dehydration concentration tower is reboiled through a steam reboiler of the hydrochloric acid dehydration concentration tower, and then enters hydrochloric acid again through a hydrochloric acid dehydration concentration conveying pump to be circularly resolved in a hydrochloric acid resolving tower.
Preferably, in the step 2, the hydrochloric acid dehydration concentration tower is kept in a negative pressure state by arranging a vacuum pump of the hydrochloric acid dehydration concentration tower.
Preferably, in the step 2, a waste acid water pump of the hydrochloric acid dehydration concentration tower is arranged on a discharge pipeline of the waste acid water tank of the hydrochloric acid dehydration concentration tower.
Preferably, in the step 1, a reboiler of the hydrochloric acid extraction distillation column is arranged at the side of the hydrochloric acid extraction distillation column to provide reboiling heat for the hydrochloric acid extraction distillation column.
The beneficial effects of the invention are as follows: the high enthalpy acid-containing water vapor generated in the hydrochloric acid extraction and stripping process is used for supplying heat to a reboiler of a hydrochloric acid dehydration concentration tower in the hydrochloric acid pressure swing rectification process, and a large amount of enthalpy taken away by the acid-containing water vapor in the extraction and stripping process in the hydrochloric acid analysis process technology is recycled to the hydrochloric acid dehydration concentration tower in the hydrochloric acid pressure swing rectification process, so that the energy consumption of the hydrochloric acid analysis process is reduced by more than 25%.
Drawings
FIG. 1 is a flow chart of the combined hydrochloric acid analysis process of the invention.
Wherein: the method comprises the steps of (1) a hydrochloric acid resolving tower, (2) a hydrochloric acid resolving tower top condenser, (3) a hydrochloric acid resolving tower hydrogen chloride gas demister, (4) a hydrochloric acid resolving tower reboiler, (5) a hydrochloric acid dehydration concentration conveying pump, (6) a hydrochloric acid dehydration concentration tower, (7) a hydrochloric acid dehydration concentration tower steam reboiler, (8) a hydrochloric acid dehydration concentration tower water vapor reboiler, (9) a hydrochloric acid dehydration concentration tower top condenser, (10) a hydrochloric acid dehydration concentration tower vacuum pump, (11) a hydrochloric acid dehydration concentration tower waste acid water tank, (12) a hydrochloric acid dehydration concentration tower waste acid water pump, (13) a calcium chloride flash tank, (14) a calcium chloride flash reboiler, (15) a calcium chloride circulating pump, (16) an extraction distillation tower top condenser, (17) an extraction distillation tower hydrogen chloride gas demister, (18) a hydrochloric acid extraction distillation tower, (19) a hydrochloric acid extraction distillation tower reboiler;
the concentration of the feed (A) is more than 23 percent of hydrochloric acid, the feed (B) of hydrochloric acid, the discharge of hydrogen chloride gas, the discharge of waste acid water (D) of 0.5 percent and the discharge of waste acid water (E) of 0.5 percent.
Detailed Description
The technical solutions of the present invention will be clearly and completely described in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Examples:
please refer to fig. 1:
step 1: resolving hydrochloric acid in a hydrochloric acid extraction and distillation tower 18 by using a calcium chloride solution as an extracting agent, wherein overhead gas is condensed by a condenser 16 at the top of the extraction and distillation tower, mist is removed by a hydrogen chloride gas demister 17 of the extraction and distillation tower to generate hydrogen chloride gas, the purity of the hydrogen chloride gas is 99.99%, the pressure is 200kPag, dilute calcium chloride extracted from a tower kettle enters a calcium chloride flash tank 13 and a calcium chloride flash reboiler 14 for heating, normal-pressure acid water vapor (the concentration of the hydrogen chloride is less than 0.5%) with the temperature of 133 ℃ and a calcium chloride solution with the concentration of about 54% with the temperature of 133 ℃ are generated after the calcium chloride is decompressed and flash-evaporated in the calcium chloride flash tank 13, the calcium chloride solution is recycled by a calcium chloride circulating pump 15 and enters the hydrochloric acid extraction and distillation tower 18 for recycling, and the hydrogen chloride extraction and distillation tower 19 is arranged at the side of the hydrochloric acid extraction and distillation tower 18 to provide reboiling heat for the hydrochloric acid extraction and distillation tower 18;
step 2: extracting 30% hydrochloric acid in a hydrochloric acid analysis tower 1, condensing tower top gas through a tower top condenser 2 of the hydrochloric acid analysis tower, removing mist through a hydrogen chloride gas demister 3 of the hydrochloric acid analysis tower to generate hydrogen chloride gas, wherein the purity of the hydrogen chloride gas is 99.99%, the pressure is 200kPag, constant boiling acid with the temperature of 141 ℃ and the concentration of about 18.5% is extracted from a tower bottom and enters a hydrochloric acid dehydration concentration tower 6 in a negative pressure state, acid-containing water vapor (the concentration of the hydrogen chloride is less than 0.5%) is produced from the tower top of the hydrochloric acid dehydration concentration tower 6, condensed through the tower top condenser 9 of the hydrochloric acid dehydration concentration tower and enters a hydrochloric acid water tank 11 of the hydrochloric acid dehydration concentration tower, concentrated hydrochloric acid with the temperature of 55 ℃ and the concentration of about 24% is extracted from the tower bottom and enters hydrochloric acid again through a hydrochloric acid dehydration concentration conveying pump 5 in the hydrochloric acid analysis tower 1 for circulating analysis;
the constant boiling acid extracted from the tower bottom of the hydrochloric acid resolving tower 1 is kept constant boiling by a reboiler 4 of the hydrochloric acid resolving tower and then enters a hydrochloric acid dehydration concentration tower 6 in a negative pressure state;
and (3) the concentrated hydrochloric acid extracted from the tower kettle of the hydrochloric acid dehydration concentration tower 6 is reboiled through a steam reboiler 7 of the hydrochloric acid dehydration concentration tower, and then enters hydrochloric acid again through a hydrochloric acid dehydration concentration conveying pump 5 to be circularly resolved in the hydrochloric acid resolving tower 1.
The vacuum pump 10 of the hydrochloric acid dehydration concentration tower is arranged to maintain the negative pressure state of the hydrochloric acid dehydration concentration tower 6.
A waste acid water pump 12 of the hydrochloric acid dehydration concentration tower is arranged on a discharge pipeline of the waste acid water tank 11 of the hydrochloric acid dehydration concentration tower;
step 3: the hydrochloric acid dehydration concentration column water vapor reboiler 8 which provides the heating function for the hydrochloric acid dehydration concentration column 6 is heated by using normal pressure acid water vapor which is generated at 133 ℃ after the pressure in the calcium chloride flash tank 13 is reduced to micro positive pressure flash evaporation in the step 1.
The water vapor reboiler 8 of the hydrochloric acid dehydration concentration tower is manufactured by using whole graphite, the tube side pressure resistance is-100 kPag, the shell side pressure resistance is 100kPag, in the existing hydrochloric acid analysis by a calcium chloride method, 1.6t of steam is required to be consumed for treating each ton of hydrochloric acid, in the existing hydrochloric acid analysis by a pressure difference analysis method, 2.2t of steam is required to be consumed for treating each ton of hydrochloric acid, the high-enthalpy water vapor generated by the flash evaporation of calcium chloride is fully recycled in the combined process, and only 1.2t of steam is required to be consumed for treating each ton of hydrochloric acid, so that the energy is saved by 25% compared with the traditional calcium chloride method, and the energy is saved by 45% compared with the pressure difference analysis method.
Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. A combined hydrochloric acid analysis process is characterized in that: the process comprises the following steps:
step 1: resolving hydrochloric acid in a hydrochloric acid extraction and distillation tower (18) by taking a calcium chloride solution as an extractant, wherein the tower top gas is condensed by a tower top condenser (16) of the extraction and distillation tower, mist is removed by a hydrogen chloride gas demister (17) of the extraction and distillation tower to generate hydrogen chloride gas, dilute calcium chloride extracted from the tower bottom enters a calcium chloride flash tank (13) and a calcium chloride flash reboiler (14) for heating, normal-pressure acidic water vapor and a calcium chloride solution are generated after decompression to micro-positive pressure flash evaporation in the calcium chloride flash tank (13), and the calcium chloride solution is recycled into the hydrochloric acid extraction and distillation tower (18) for recycling by a calcium chloride circulating pump (15);
step 2: extracting hydrochloric acid in a hydrochloric acid resolving tower (1), wherein tower top gas is condensed by a tower top condenser (2) of the hydrochloric acid resolving tower, mist is removed by a hydrogen chloride gas demister (3) of the hydrochloric acid resolving tower to generate hydrogen chloride gas, constant boiling acid extracted from a tower bottom enters a hydrochloric acid dehydration concentration tower (6) in a negative pressure state, acid-containing water vapor produced by the tower top of the hydrochloric acid dehydration concentration tower (6) is condensed by a tower top condenser (9) of the hydrochloric acid dehydration concentration tower and then enters a waste acid tank (11) of the hydrochloric acid dehydration concentration tower, and concentrated hydrochloric acid extracted from a tower bottom enters hydrochloric acid in the hydrochloric acid resolving tower (1) again through a hydrochloric acid dehydration concentration conveying pump (5) for cyclic resolution;
step 3: a water vapor reboiler (8) of the hydrochloric acid dehydration concentration tower for providing a heating function for the hydrochloric acid dehydration concentration tower (6) is heated by generating normal-pressure acid water vapor after the pressure in a calcium chloride flash tank (13) in the step 1 is reduced to micro-positive pressure flash evaporation;
in the step 2, constant boiling acid extracted from the tower bottom of the hydrochloric acid resolving tower (1) is kept constant boiling by a reboiler (4) of the hydrochloric acid resolving tower and then enters a hydrochloric acid dehydration concentration tower (6) in a negative pressure state;
in the step 2, concentrated hydrochloric acid extracted from the tower kettle of the hydrochloric acid dehydration concentration tower (6) is reboiled through a steam reboiler (7) of the hydrochloric acid dehydration concentration tower, and then enters hydrochloric acid again through a hydrochloric acid dehydration concentration conveying pump (5) to be circularly analyzed in a hydrochloric acid analysis tower (1).
2. The combined hydrochloric acid resolution process of claim 1, wherein: in the step 1, the gas at the top of the hydrochloric acid extraction distillation column (18) is condensed by a condenser (16) at the top of the extraction distillation column, and then mist is removed by a hydrogen chloride gas demister (17) of the extraction distillation column to generate hydrogen chloride gas with the purity of 99.99 percent; in the step 2, hydrochloric acid is extracted in the hydrochloric acid analysis tower (1), wherein the tower top gas is condensed by a tower top condenser (2) of the hydrochloric acid analysis tower and then is defogged by a hydrogen chloride gas defogger (3) of the hydrochloric acid analysis tower, and the purity of the generated hydrogen chloride gas is 99.99%.
3. A combined hydrochloric acid resolution process as claimed in claim 2, wherein: in the step 1, the temperature of the extracting agent calcium chloride solution is 133 ℃, and the concentration of the extracting agent calcium chloride solution is 50% -60%.
4. A combined hydrochloric acid resolution process as claimed in claim 3, wherein: in the step 2, the concentration of the raw material hydrochloric acid entering the hydrochloric acid analysis tower (1) is at least 23 percent.
5. The combined hydrochloric acid resolution process of claim 1, wherein: in the step 2, the hydrochloric acid dehydration concentration tower (6) is kept in a negative pressure state by arranging a vacuum pump (10) of the hydrochloric acid dehydration concentration tower.
6. The combined hydrochloric acid resolution process of claim 1, wherein: in the step 2, a waste acid water pump (12) of the hydrochloric acid dehydration concentration tower is arranged on a discharge pipeline of the waste acid water tank (11) of the hydrochloric acid dehydration concentration tower.
7. The combined hydrochloric acid resolution process of claim 1, wherein: in the step 1, a reboiler (19) of the hydrochloric acid extraction distillation column is arranged at the side of the hydrochloric acid extraction distillation column (18) to provide reboiling heat for the hydrochloric acid extraction distillation column (18).
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| CN115180594B (en) * | 2022-07-11 | 2023-12-26 | 新疆西部合盛硅业有限公司 | Recovery process of wastewater from organosilicon slurry residue treatment |
| CN115991457A (en) * | 2023-02-24 | 2023-04-21 | 中国矿业大学 | Recovery device and recovery method for hydrochloric acid in chlorination distillation waste acid |
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| CN214383703U (en) * | 2021-01-20 | 2021-10-12 | 杭州东日节能技术有限公司 | Low-concentration impurity-containing dilute hydrochloric acid hydrogen chloride purification device by sulfuric acid method |
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2022
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| RU1790587C (en) * | 1990-12-04 | 1993-01-23 | Физико-Химический Институт Им.А.В.Богатского Ан@ Усср | Indicating flomaster composition for controlling sterilization with ethylene oxide |
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| WO2018204764A1 (en) * | 2017-05-05 | 2018-11-08 | Camp4 Therapeutics Corporation | Identification and targeted modulation of gene signaling networks |
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