CN102351149B - System for recovering and removing chlorine from hydrogen chloride - Google Patents
System for recovering and removing chlorine from hydrogen chloride Download PDFInfo
- Publication number
- CN102351149B CN102351149B CN 201110180587 CN201110180587A CN102351149B CN 102351149 B CN102351149 B CN 102351149B CN 201110180587 CN201110180587 CN 201110180587 CN 201110180587 A CN201110180587 A CN 201110180587A CN 102351149 B CN102351149 B CN 102351149B
- Authority
- CN
- China
- Prior art keywords
- tower
- chlorine
- alkali lye
- tail gas
- hydrogen chloride
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
The invention provides a system for recovering and removing chlorine from hydrogen chloride, comprising a pipeline deduster, an integrated absorption tower, a vitriol drying tower, a concentrated acid cooler, a tail gas alkaline washing tower, an alkali lye cooling tower, and an alkali lye circulation tank. According to the invention, dust is removed from the hydrogen chloride mixed gas containing chlorine through the pipeline deduster, then the hydrogen chloride mixed gas containing chlorine passes through the integrated absorption tower, hydrogen chloride dissolves in water to form a hydrochloric acid solution with the concentration of 28-38 %, and the hydrochloric acid solution flows out through the concentrated acid cooler; the flow direction of the tail gas is divided into two paths, most tail gas flows to the vitriol drying tower and is recovered after drying, and little tail gas flows to the tail gas alkaline washing tower; and the tail gas alkaline washing tower, the alkali lye cooling tower, and the alkali lye circulation tank form a circulation system. By processing with the system disclosed herein, the separation of chlorine from hydrogen chloride is thorough, the rate of recovery is high, the purity of the hydrochloric acid solution is high, and the pollution of tail gas is little. The system has the advantages of high efficiency and long service life, and is suitable for large scale industrial operation.
Description
Technical field
The present invention relates to contain the tripping device of the hydrogen chloride gas gas mixture of a small amount of chlorine, one of the technological problems that must resolve during to be that hydrogenchloride is synthetic produce.
Background technology
Usually the removal chlorine method that contains the chlorine hydride mixed gas employing of chlorine has following several:
(1) with saturated sodium sulfite aqueous cleaning gas mixture, utilize redox reaction to remove chlorine.The method need to consume S-WAT, and can not reclaim chlorine, and cost is higher.
(2) by saturated nacl aqueous solution, heated solution can obtain the mixed gas of hydrogenchloride and water vapour, and is dry by Vanadium Pentoxide in FLAKES at last, obtains pure hydrogen chloride gas first with hydrogen fully burning in mixed gas, and then with mixed gas.The method need to consume hydrogen, sodium-chlor, Vanadium Pentoxide in FLAKES etc., and process is complicated.
(3) according to the difference of hydrogenchloride and chlorine fusing point, carry out low ternperature separation process.The method energy consumption is excessive.
(4) pass into methane in gas mixture, under illumination, methane and chlorine generation chain reaction, generating under normal temperature is the tetracol phenixin of liquid, remaining gas is hydrogenchloride.Because tetracol phenixin is hazardous chemical, the method security is bad, and hydrogenchloride may be sneaked into excessive methane gas.
Number of patent application is that 200510025910.6 file discloses " a kind of separating and purifying method that contains chlorine and hydrogenchloride mix waste gas ".Adopt solvent orange 2 A with the chlorine absorption in mix waste gas in liquid phase, HCl separation with gas phase, solvent orange 2 A desorb after absorption chlorine obtains chlorine, solvent orange 2 A is a kind of in benzene, silicon tetrachloride, nonane, sulfur monochloride, tetracol phenixin, chlorsulfonic acid, remove solvent orange 2 A in the hydrogenchloride gas phase with solvent B, just obtain hydrogen chloride gas, solvent B is that ring is penta 2 rare, a kind of in the chlordene butadiene.Hydrogen chloride gas is removed micro-content organism with the concentrated hydrochloric acid washing, then removes heavy metal element through chemical washing, and water absorbs makes hydrochloric acid.The method needs multiple auxiliary organic solvent, and not environmental protection is uneconomical.
Summary of the invention
Goal of the invention: overcome the many disadvantages of separating chlorine gas method in traditional hydrogen chloride gas, provide a kind of separation thorough, the removal of the chlorine from hydrogen chloride that the chlorine recovery utilization rate is high and recovery system.
Technical scheme: for realizing purpose of the present invention, the removal of chlorine from hydrogen chloride provided by the invention and recovery system, contain chlorine and separate the integrated absorption tower of removing from hydrogenchloride, also contain dust remover for pipeline, sulfuric acid tower, concentrated acid water cooler, tail gas alkaline cleaning tower, alkali lye cooling tower, alkali lye circulation tank.
Be that the chlorine hydride mixed gas body of 1%-10% chlorine is when being inputted by the gas mixture intake line when containing mass ratio, first remove the solid particulates such as dust by dust remover for pipeline, the integrated absorption tower of then flowing through, the spout at integrated absorption tower top has the water spray, the cooling rear outflow of concentrated acid water cooler of flowing through of the hydrochloric acid soln of the water-soluble one-tenth concentration of hydrogenchloride in gas mixture 28%-38%, hydrochloric acid soln.
Chlorine solubleness in water is lower, contains most chlorine and a small amount of aqueous vapor in remaining tail gas, contains hardly hydrogenchloride.Exhaust gas flow direction is divided into two-way: when equipment normally moved, switch 1 was opened, and switch 2 cuts out, and exhaust gas flow direction vitriol oil drying tower reclaims chlorine after drying is processed; During the equipment initial launch or before finishing operation, switch 2 is opened, switch 1 cuts out, the exhaust gas flow direction tail gas alkaline cleaning tower of this moment.
Described dust remover for pipeline preferably has 2, is connected in parallel in the gas mixture intake line, and during a job, another is standby.
The inwall of described integrated absorption tower is preferably made by graphite, and erosion resistance is better.
The vitriol oil concentration of described sulfuric acid tower can be 70%-98%, preferred 98% the vitriol oil.
After described drying is processed, recovery chlorine in hydrogen cloride concentration＜50ppm of containing, purity of chlorine gas feeding is high.
Also contain the alkali lye circulation tank in system, described tail gas alkaline cleaning tower, alkali lye cooling tower, alkali lye circulation tank form a recycle system, and the alkali lye circulation tank is connected with alkali lye supply pipe, and the recycle system is connected with the waste liquid vent pipe.In described alkali lye circulation tank, alkali lye can be calcium hydroxide, sodium hydroxide or potassium hydroxide aqueous solution.Alkali 20% calcium hydroxide aqueous solution preferably in described alkali lye circulation tank.
Described integrated absorption tower, concentrated acid water cooler, alkali lye cooling tower are connected with the water coolant inlet and outlet pipe lines respectively, carry out respectively cooling to the absorption reaction heat of acid solution or alkali lye.Described cold in-water temperature can be normal temperature to 35 ℃, and leaving water temperature(LWT) can be 35 ℃-45 ℃.
The main raw that described sulfuric acid tower is made is acidproof PVC and FRP; The main raw that tail gas alkaline cleaning tower and alkali lye circulation tank are made is alkaline-resisting PVC and FRP; Good corrosion resistance, and cost is lower.
Beneficial effect: through the processing of system of the present invention, chlorine and HCl separation are more thorough, the hydrogen cloride concentration＜50ppm that contains in the chlorine of discharge, and the chlorine recovery utilization rate is high; Concentration of hydrochloric acid solution is high, purity is high; The vent gas treatment environmental protection is polluted few; After heating up, water coolant can be used as the thermal source of other purposes.In system, all parts is easy to maintenance, and is safe and reliable, and efficient is secure, and the life-span is permanent, is fit to the heavy industrialization operation and uses.
Description of drawings
Accompanying drawing is a structure of the present invention and schematic flow sheet.
In figure, 1, integrated absorption tower, dust remover for pipeline, sulfuric acid tower, concentrated acid water cooler, tail gas alkaline cleaning tower,, alkali lye cooling tower, alkali lye circulation tank, switch 1 open, switch 2, pipeline, cooling water inlet pipe road, cooling water outlet pipe road.
Embodiment
Below, in conjunction with the accompanying drawings and embodiments the present invention is made more specific description.
Choose corresponding component integrated absorption tower, also contain dust remover for pipeline, sulfuric acid tower, concentrated acid water cooler, tail gas alkaline cleaning tower,, alkali lye cooling tower, alkali lye circulation tank, switch 1 open, switch 2, many pipelines, 3 water coolant inlet and outlet pipe lines, many pipe valves.
Be that the chlorine hydride mixed gas body of 1%-10% chlorine is when being inputted by the gas mixture intake line when containing mass ratio, first remove the solid particulates such as dust by dust remover for pipeline, the integrated absorption tower of then flowing through, the spout at integrated absorption tower top has the water spray, the cooling rear outflow of concentrated acid water cooler of flowing through of the hydrochloric acid soln of the water-soluble one-tenth concentration of hydrogenchloride in gas mixture 28%-38%, hydrochloric acid soln;
Chlorine solubleness in water is lower, contains most chlorine and a small amount of aqueous vapor in remaining tail gas, contains hardly hydrogenchloride; Exhaust gas flow direction is divided into two-way: when equipment normally moved, switch 1 was opened, and switch 2 cuts out, and exhaust gas flow direction vitriol oil drying tower reclaims chlorine after drying is processed; Equipment initial launch, end move front or take a sample when moving, and switch 2 is opened, and switch 1 cuts out, exhaust gas flow direction tail gas alkaline cleaning tower at this moment.
Embodiment 1:
Contain mass ratio and be the chlorine hydride mixed gas body of 3% chlorine by the gas mixture intake line, described dust remover for pipeline is connected in the gas mixture intake line.The inwall of described integrated absorption tower is made by graphite.The vitriol oil concentration of described sulfuric acid tower is 80%.The cooling rear outflow of concentrated acid water cooler of flowing through of the hydrochloric acid soln of the water-soluble one-tenth concentration 31% of the hydrogenchloride in described gas mixture, hydrochloric acid soln.After processing, described drying reclaims the hydrogen cloride concentration＜50ppm that contains in chlorine.Described integrated absorption tower, concentrated acid water cooler, alkali lye cooling tower are connected with respectively the water coolant inlet and outlet pipe lines.Described cold in-water temperature is normal temperature, and leaving water temperature(LWT) is 35 ℃-45 ℃.
Embodiment 2: contain mass ratio and be the chlorine hydride mixed gas body of 5% chlorine by the gas mixture intake line, described dust remover for pipeline has 2, is connected in parallel in the gas mixture intake line, and during a job, another is standby.The inwall of described integrated absorption tower is made by graphite.The vitriol oil concentration of described sulfuric acid tower is 98%.The hydrochloric acid soln of the water-soluble one-tenth concentration of hydrogenchloride in gas mixture 30%-35%, hydrochloric acid soln are flowed through and are reclaimed the hydrogen cloride concentration＜30ppm that contains in chlorine after the described drying of the cooling rear outflow of concentrated acid water cooler is processed.Also contain the alkali lye circulation tank in described system, described tail gas alkaline cleaning tower, alkali lye cooling tower, alkali lye circulation tank form a recycle system, and the alkali lye circulation tank is connected with alkali lye supply pipe, and the recycle system is connected with the waste liquid vent pipe; In described alkali lye circulation tank, alkali lye is 20% calcium hydroxide aqueous solution.Described integrated absorption tower, concentrated acid water cooler, alkali lye cooling tower are connected with respectively the water coolant inlet and outlet pipe lines.32 ℃ of cold in-water temperatures, leaving water temperature(LWT) are 38 ℃ of left and right.
Claims (4)
1. the removal of a chlorine from hydrogen chloride and recovery system, contain chlorine and separate the integrated absorption tower of removing from hydrogenchloride, it is characterized in that: also contain dust remover for pipeline, sulfuric acid tower, concentrated acid water cooler, tail gas alkaline cleaning tower, alkali lye cooling tower;
Be that the chlorine hydride mixed gas body of 1%-10% chlorine is when being inputted by the gas mixture intake line when containing mass ratio, first remove the solid particulates such as dust by dust remover for pipeline, the integrated absorption tower of then flowing through, the spout at integrated absorption tower top has the water spray, the cooling rear outflow of concentrated acid water cooler of flowing through of the hydrochloric acid soln of the water-soluble one-tenth concentration of hydrogenchloride in gas mixture 28%-38%, hydrochloric acid soln;
Chlorine solubleness in water is lower, contains most chlorine and a small amount of aqueous vapor in remaining tail gas, contains hardly hydrogenchloride; Exhaust gas flow direction is divided into two-way: when equipment normally moved, switch 1 was opened, and switch 2 cuts out, and exhaust gas flow direction vitriol oil drying tower reclaims chlorine after drying is processed; During the equipment initial launch or before finishing operation, switch 2 is opened, switch 1 cuts out, the exhaust gas flow direction tail gas alkaline cleaning tower of this moment;
Described dust remover for pipeline has 2, is connected in parallel in the gas mixture intake line, and during a job, another is standby;
The inwall of described integrated absorption tower is made by graphite; The main raw that described sulfuric acid tower is made is acidproof PVC and FRP; The main raw that tail gas alkaline cleaning tower and alkali lye circulation tank are made is alkaline-resisting PVC and FRP;
Described integrated absorption tower, concentrated acid water cooler, alkali lye cooling tower are connected with respectively the water coolant inlet and outlet pipe lines; Described cold in-water temperature is normal temperature to 35 ℃, and leaving water temperature(LWT) is 35 ℃-45 ℃;
The vitriol oil concentration of described sulfuric acid tower is 70%-98%.
2. the removal of chlorine from hydrogen chloride according to claim 1 and recovery system, is characterized in that: reclaim the hydrogen cloride concentration＜50ppm that contains in chlorine after described drying is processed.
3. the removal of chlorine from hydrogen chloride according to claim 1 and recovery system, it is characterized in that: also contain the alkali lye circulation tank in system, described tail gas alkaline cleaning tower, alkali lye cooling tower, alkali lye circulation tank form a recycle system, the alkali lye circulation tank is connected with alkali lye supply pipe, and the recycle system is connected with the waste liquid vent pipe; In the alkali lye circulation tank, alkali lye is calcium hydroxide, sodium hydroxide or potassium hydroxide aqueous solution.
4. the removal of chlorine from hydrogen chloride according to claim 3 and recovery system, it is characterized in that: in described alkali lye circulation tank, alkali lye is 20% calcium hydroxide aqueous solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110180587 CN102351149B (en) | 2011-06-30 | 2011-06-30 | System for recovering and removing chlorine from hydrogen chloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110180587 CN102351149B (en) | 2011-06-30 | 2011-06-30 | System for recovering and removing chlorine from hydrogen chloride |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102351149A CN102351149A (en) | 2012-02-15 |
| CN102351149B true CN102351149B (en) | 2013-06-05 |
Family
ID=45574835
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110180587 Active CN102351149B (en) | 2011-06-30 | 2011-06-30 | System for recovering and removing chlorine from hydrogen chloride |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102351149B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113387918A (en) * | 2021-06-19 | 2021-09-14 | 济宁正旺生物科技有限公司 | Method for recycling unreacted chlorine in synthesis of chlorinated ethylene carbonate |
| CN114797708B (en) * | 2022-05-23 | 2024-02-20 | 倪治法 | Deacidification circulating system and deacidification process |
| CN116715191B (en) * | 2023-08-08 | 2023-10-27 | 浙江百能科技有限公司 | Sulfuric acid phase decomposition process and system for cyclic hydrogen production by sulfur and iodine |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE631187A (en) * | 1962-04-19 | |||
| CN100464820C (en) * | 2006-03-13 | 2009-03-04 | 董谊仁 | Gas-purifying combined absorbing tower and application thereof |
| CN100562487C (en) * | 2007-06-29 | 2009-11-25 | 杭州中昊科技有限公司 | The complete recovering technique of hydrogenchloride in the industrial gasses |
| CN100582066C (en) * | 2007-10-16 | 2010-01-20 | 南京工业大学 | Process for producing ethylene by ethanol dehydration |
| CN101219920A (en) * | 2008-01-16 | 2008-07-16 | 南京工业大学 | Ethanol dehydration technique adopting molecular sieve catalyst |
| CN201317749Y (en) * | 2008-12-25 | 2009-09-30 | 浙江恒业成有机硅有限公司 | Methyl chloride purification buffer tank device |
| CN101513585B (en) * | 2009-03-02 | 2012-06-27 | 浙江富士特硅材料有限公司 | Device for recycling tail gas in production of gas-phase silica |
-
2011
- 2011-06-30 CN CN 201110180587 patent/CN102351149B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN102351149A (en) | 2012-02-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105084370B (en) | A kind of slurry treating method and apparatus in cold hydrogenation process | |
| AU2010295259B2 (en) | Thermal distillation system and process | |
| CN102705839A (en) | Incineration disposal system of fluorine-containing waste liquid and waste gas and disposal method thereof | |
| CN103471402A (en) | Method of recovering flue gas waste heat and dust in reclaimed copper refining | |
| CN102351149B (en) | System for recovering and removing chlorine from hydrogen chloride | |
| CN105923610B (en) | Acetylene cleaning acid regeneration technique | |
| CN104495953A (en) | Process for treating industrial waste hydrochloric acid in recycling way through salt fractionation method | |
| CN104649335A (en) | Method and device for recycling ferrous chloride crystal and hydrochloric acid from chlorohydric acid pickling waste solution | |
| CN113398719A (en) | Device and method for recovering chlorine in tail chlorine | |
| CN204588694U (en) | A kind of production system of used in electronic industry hydrofluoric acid | |
| CN105836706A (en) | Method for preparing hydrogen gas by hot aluminum slag/vapor combined reaction | |
| CN209155563U (en) | A kind of residual neat recovering system of solid water glass dissolution | |
| WO2013159530A1 (en) | Method for reusing excess oxygen and recycling carbon dioxide in supercritical water oxidation system | |
| CN110451596A (en) | A kind of carrier gas extraction HPE vapo(u)rization system | |
| CN105000745B (en) | A kind of sulfur Gas Fields produced water treatment system | |
| CN115448330B (en) | System and process for recycling and separating chloride salt in flue gas after plasma melting of fly ash | |
| CN108314119A (en) | Desulfurization wastewater phase transformation flash crystallization Zero discharging system and method for treating desulfurized wastewater | |
| CN102745652B (en) | Technology for producing sulphuric acid purification feed gas by using medium or low concentration waste acid | |
| CN210874758U (en) | Waste circuit board smelting flue gas purification and recovery system | |
| CN203922727U (en) | A kind of dense spent acid is produced sulfuric acid purification unstripped gas system | |
| CN201906471U (en) | Vacuum concentration device for diluted acid | |
| CN104016311B (en) | A kind of dense spent acid produces sulfuric acid purification unstripped gas system | |
| CN205773843U (en) | Acid-bearing wastewater processing equipment | |
| CN203683144U (en) | Device of recovering ferrous chloride crystals and hydrochloric acid from hydrochloric acid pickling wastewater | |
| CN204825007U (en) | Condensing equipment is retrieved to mercury |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20120215 Assignee: Nantong Long Trust Graphite Science and Technology Development Co., Ltd. Assignor: Chou Xiaofeng Contract record no.: 2013320000476 Denomination of invention: System for recovering and removing chlorine from hydrogen chloride License type: Exclusive License Record date: 20130531 |
|
| LICC | Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20201130 Address after: 226500 Jiangsu province Nantong City Jiuhua town Rugao City Huaxing Road No. 8 Patentee after: Nantong star graphite Co.,Ltd. Address before: 226011, Nantong District, Jiangsu City, Gangzha Province Qin Zhao street Xi'an Bridge Village 15 groups Patentee before: Qiu Xiaofeng |
|
| TR01 | Transfer of patent right |