CN105273760A - Waste water zero-discharge acetylene production technology - Google Patents
Waste water zero-discharge acetylene production technology Download PDFInfo
- Publication number
- CN105273760A CN105273760A CN201410691882.0A CN201410691882A CN105273760A CN 105273760 A CN105273760 A CN 105273760A CN 201410691882 A CN201410691882 A CN 201410691882A CN 105273760 A CN105273760 A CN 105273760A
- Authority
- CN
- China
- Prior art keywords
- acetylene
- tower
- water
- desorption
- producer
- 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.)
- Pending
Links
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 title claims abstract description 101
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 title claims abstract description 99
- 239000002351 wastewater Substances 0.000 title claims abstract description 43
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 31
- 238000005516 engineering process Methods 0.000 title abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000000034 method Methods 0.000 claims abstract description 31
- 239000002002 slurry Substances 0.000 claims abstract description 27
- 239000002893 slag Substances 0.000 claims abstract description 26
- 239000005997 Calcium carbide Substances 0.000 claims abstract description 23
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000003795 desorption Methods 0.000 claims abstract description 19
- 238000004140 cleaning Methods 0.000 claims abstract description 11
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims abstract description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical group C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 66
- 239000011734 sodium Substances 0.000 claims description 66
- 229910052708 sodium Inorganic materials 0.000 claims description 66
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims description 20
- 239000000460 chlorine Substances 0.000 claims description 20
- 229910052801 chlorine Inorganic materials 0.000 claims description 20
- 239000012535 impurity Substances 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 7
- 239000003513 alkali Substances 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000012065 filter cake Substances 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- 239000007844 bleaching agent Substances 0.000 claims description 4
- 239000002131 composite material Substances 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000000706 filtrate Substances 0.000 claims description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 1
- 239000005864 Sulphur Substances 0.000 claims 1
- 239000011574 phosphorus Substances 0.000 claims 1
- 229910052698 phosphorus Inorganic materials 0.000 claims 1
- 238000003825 pressing Methods 0.000 claims 1
- 239000007787 solid Substances 0.000 claims 1
- 238000001816 cooling Methods 0.000 abstract description 16
- 239000006228 supernatant Substances 0.000 abstract description 12
- 239000005708 Sodium hypochlorite Substances 0.000 abstract 3
- 238000013329 compounding Methods 0.000 abstract 2
- 230000007613 environmental effect Effects 0.000 abstract 1
- 230000007704 transition Effects 0.000 abstract 1
- 239000002699 waste material Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 34
- 230000000052 comparative effect Effects 0.000 description 6
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- DIWKDXFZXXCDLF-UHFFFAOYSA-N chloroethyne Chemical group ClC#C DIWKDXFZXXCDLF-UHFFFAOYSA-N 0.000 description 1
- 230000002939 deleterious effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 239000004800 polyvinyl chloride Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- JBJWASZNUJCEKT-UHFFFAOYSA-M sodium;hydroxide;hydrate Chemical compound O.[OH-].[Na+] JBJWASZNUJCEKT-UHFFFAOYSA-M 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
Landscapes
- Removal Of Specific Substances (AREA)
Abstract
The invention relates to a wet method production technology for preparing acetylene from calcium carbide. Crude acetylene from a generator needs a large volume of sodium hypochlorite solution for cleaning, After the generated waste sodium hypochlorite solution goes through a first desorption tower and acetylene is recovered, part of the solution is used for compounding of a sodium hypochlorite solution, and part of the solution goes through a transition tank and goes into a concentration tank for reuse. Through adjusting of the compounding proportion, all the waste water generated in the technology can be reused without discharge. After a diluted calcium carbide slag slurry overflowed from the generator goes through a second desorption tower and acetylene is recovered, the diluted calcium carbide slag slurry goes into the concentration tank for concentration; the supernatant in the concentration tank is cooled in water cooling tower, a heat exchanger is added in front of an acetylene generator, circulating water cooling is carried out, stable water input temperature and water inflow of the acetylene generator are ensured, and the stability and the controllability of technology production are raised. The provided technology raises the acetylene yield, ensures water balance, achieves waste water zero discharge and has good economic and environmental protection benefits compared with traditional technologies.
Description
Technical field
The present invention relates to a kind of wet processing of calcium carbide method acetylene production, this technique achieves the complex process of useless clorox, thus make the waste water of this technique reach zero release, reclaim the acetylene in calcium carbide shoddye slurry simultaneously, be specially adapted to the acetylene unit in generated by polyvinyl chloride by calcium carbide production technique.
Background technology
Acetylene production process is mainly divided into calcium carbide route and ethylene process, and calcium carbide route is divided into again dry method and wet method.It is domestic at present that what generally apply is calcium carbide method acetylene production wet processing.As everyone knows, calcium carbide and water react, and generate acetylene and release a large amount of heat, reactional equation is shown below.
CaC
2+2H
2O→C
2H
2+Ca(OH)
2+129.8kJ/mol
Owing to often containing the impurity such as a small amount of sulfide, phosphide in calcium carbide, can containing impurity such as a small amount of phosphuret-(t)ed hydrogen, hydrogen sulfide in the acetylene gas produced, need that acetylene gas is carried out washing peace and quiet, Fig. 1 describes industrial traditional calcium carbide and produces the wet processing of acetylene: first added by the calcium carbide that fragmentation is good in producer to react with water and generate acetylene gas, the water added in producer is a large amount of, so that water can take away the heat that reaction produces, generate a large amount of carbide slag slurries simultaneously; Thick acetylene gas through water wash column spray, washing, cooling, generally by compressor compresses to 50kPa(gauge pressure) about, send into peace and quiet tower to remove the impurity such as phosphuret-(t)ed hydrogen, hydrogen sulfide in acetylene; After alkali cleaning, cooling demist, obtain high purity acetylene gas, send into gas holder or next production process.
The temperature of the water added in producer is very crucial processing parameter, when other processing parameter keeps stable (temperature, pressure as producer), which determine the added water yield, the water yield determines the amount of carbide slag slurries and the change of composition thereof, and then affects the foreign matter content in thick acetylene gas.Chinese patent application 201080048301.1 " acetylene generation equipment, the control method of acetylene generation equipment and the manufacture method of acetylene gas " proposes the control device that a kind of flow and temperature by detecting acetylene gas controls the flow being supplied to carbide-feed generator water.
The impurity such as the phosphuret-(t)ed hydrogen in thick acetylene gas, hydrogen sulfide can be oxidized to acid by the oxidisability of the vitriol oil or clorox (hereinafter referred to as secondary sodium) solution and be removed, and current domestic enterprise generally uses the latter.It is well known that work as the available chlorine < 0.05% of time sodium solution, during pH value > 8, peace and quiet deleterious, and available chlorine > 0.15%(is particularly low at PH) time easily generate explosive substance chloroacetylene, therefore the available chlorine general control of the secondary sodium solution of acetylene cleaning is 0.08 ~ 0.12%, and pH value controls 7 ~ 8.Because the available chlorine in secondary sodium solution is very low, the secondary sodium solution amount of peace and quiet process need is very large, if the secondary sodium solution after peace and quiet can not reuse, then can produce a large amount of secondary sodium waste water, and the acetylene about 1 ~ 1.5g/L dissolved in secondary sodium waste water, there is very important economic worth.Chinese patent application 200910064330.6 proposes a kind of reuse method secondary sodium waste water being cooled rear feeding producer; Chinese patent application 201010173529.5 proposes the method for a kind of sodium waste water closed cycle, first secondary sodium waste water NaOH solution regulates pH value to be 6 ~ 12 by the method, then lower the temperature and add impurity, the suspended substance sedimentation that chemical agent makes in time sodium waste water, supernatant fluid reuse is in the preparation of fresh sodium solution, and the concentrated solution of sedimentation send sludge treating system; Chinese patent application 200810096505.7 proposes the method for a kind of sodium waste water circulation preparation time sodium solution, and the party comprises need first by the acetylene removal in secondary sodium waste water, then by secondary sodium waste water and the fresh secondary sodium solution of dense sodium mixed preparing.
Not only containing the acetylene dissolved from carbide-feed generator carbide slag slurries out, the more important thing is and can contain many undecomposed small electric stone granulates, the surface of these calcium carbide particles " is wrapped up in attached " by carbide slag slurries, causes the reaction of calcium carbide and water incomplete.Chinese patent application 200710306215.6 proposes a kind of Technology extracting residual acetylene gas in carbide-feed generator carbide slag slurries.
The object of the invention is to propose that a kind of acetylene yield is high, the acetylene from calcium carbide production technique of wastewater zero discharge.
Summary of the invention
The acetylene production process of a kind of wastewater zero discharge that the present invention proposes, comprise the device such as acetylene generation, acetylene cleaning, the recovery of slag slurry acetylene, secondary sodium waste water acetylene reclaims, secondary sodium is composite, slag slurry thickening filtration, Fig. 2 describes technical process of the present invention: from producer acetylene gas out, successively after the operations such as washing, compression, peace and quiet, alkali cleaning, cooling, obtain high purity acetylene, enter gas holder or next production process; Acetylene cleaning adopts the double-column process of pressurization, namely available chlorine be 0.01% ~ 0.12%, pH value be 7 ~ 8 fresh sodium solution be introduced into the peace and quiet acetylene gas of peace and quiet two tower, continue again to enter a peace and quiet tower, secondary sodium waste water flows out from a peace and quiet tower tower reactor, and available chlorine, about 0.06%, enters desorption one tower, through spray desorption under condition of negative pressure, after removing acetylene gas, a part removes time sodium compositional apparatus, and a part goes aqueduct to enter concentration basin; A large amount of carbide slag slurries that producer produces enter desorption two tower and remove acetylene gas, and then enter concentration basin by aqueduct, the supernatant liquor of concentration basin enters clean solution tank, tentatively cools through water cooling tower, then enters after circulating water in producer; The filter cake entrucking obtained after carbide slag slurries pressure filter press filtration after concentrated, filtrate is back to concentration basin, filter cake moisture about 38% ~ 42%.
The acetylene production process of described a kind of wastewater zero discharge, the water added in producer is from the supernatant liquor of concentration basin, this supernatant liquor in clean solution tank after water cooling tower cooling with pump delivery to interchanger, producer is entered after being cooled to 25 ~ 30 DEG C, the temperature of this supernatant is preferably made to remain on 25 DEG C, the present invention is after increase interchanger, the water temperature entering producer is no longer subject to the impact of seasonal variation or weather, inflow temperature is constant, ensure that the water yield entering producer is constant, thus make follow-up all production operations constant, i.e. whole stable processing technique, not affected by environment.
The acetylene production process of described a kind of wastewater zero discharge, the pressure general control at carbide-feed generator top is at 0.004 ~ 0.012MPa, and temperature of reaction controls at 80 ~ 90 DEG C.
The acetylene production process of described a kind of wastewater zero discharge, spray under condition of negative pressure respectively by desorption one tower and desorption two tower and remove and reclaim the acetylene gas dissolved in time sodium waste water and carbide slag slurries, its negative pressure device is the water ring vacuum pump and the gas-liquid separator that connect desorption tower top, liquid distributor is had in desorption tower, the vacuum tightness of desorption tower is 10kPa ~ 70kPa, preferred 40kPa ~ 70kPa.
The acetylene production process of described a kind of wastewater zero discharge, the secondary sodium waste water part removing acetylene removes time sodium compositional apparatus, and another part enters concentration basin through ramp pan together with carbide slag slurries, goes composite ratio to account for 20% ~ 80% of whole waste water.
The acetylene production process of described a kind of wastewater zero discharge, in secondary sodium solution process for preparation, dense sodium elder generation of available chlorine 10% and the raw water Homogeneous phase mixing in 1# Venturi reactor that disappears, obtain the centre time sodium solution that available chlorine is 0.15 ~ 0.5%; Middle time sodium solution and the secondary sodium waste water Homogeneous phase mixing in 2# Venturi reactor removing acetylene, obtain fresh the sodium solution that available chlorine is 0.1% ~ 0.12%, at 2# Venturi reactor, PH measuring apparatus is installed simultaneously, control by volume pump the amount adding acid or alkali, make the pH value of fresh sodium solution 7 ~ 8.
Technological design reasonable benefit/risk of the present invention, the secondary sodium waste water fully recovering of peace and quiet generation, system water entrance only has secondary sodium process for preparation, and the water balance that the water yield of system and clear liquid working cycle are lost taken out of by the water yield that the required water yield and acetylene occur to consume, filter cake, do not have discharge of wastewater; Reclaim the acetylene in carbide slag slurries and time sodium waste water simultaneously, improve acetylene yield; Control inflow temperature before producer not by the impact of environment, the processing parameter of whole production process is stablized, is conducive to management and the control of production process.
Accompanying drawing explanation
Fig. 1 is the FB(flow block) of traditional acetylene from calcium carbide production technique.
Fig. 2 is the acetylene from calcium carbide technological process of production block diagram that the present invention proposes.
Specific embodiments
Following comparative example and embodiment are to explanation of the present invention, but the present invention is not limited to this.
comparative example 1:
As shown in Figure 1, the power and water stone from clean solution tank adds in carbide-feed generator with set flow simultaneously, and keep the pressure and temperature of producer in set(ting)value, the calcium carbide in producer and water react, and generate acetylene gas and carbide slag slurries; Acetylene gas from producer top successively through washing, compression after, enter acetylene cleaning post, with available chlorine be 0.1% ~ 0.12%, pH value be 7 ~ 8 fresh sodium solution remove the impurity such as hydrogen sulfide and phosphuret-(t)ed hydrogen in acetylene gas, secondary sodium waste water enters concentration basin through aqueduct; Acetylene gas enters gas holder or next production process again after alkali cleaning, cooling; The carbide slag slurries overflowed from producer enters concentration basin through aqueduct, and supernatant liquor enters clean solution tank, directly sends in producer, supernatant liquor temperature about 45 DEG C (summer) after water cooling tower cooling with pump.
Secondary sodium waste water and carbide slag slurries through aqueduct to the sedimentation in concentration basin, concentration basin and supernatant liquor in the process of cooling of water cooling tower, the acetylene dissolved and unreacted calcium carbide are because draining into air or losing with slag slurry.
Available chlorine be 0.1% ~ 0.12% fresh sodium with 10% dense sodium and the raw water preparation that disappears, the amount (bringing production system into) of the required raw water that disappears is far away higher than the water yield (reaction consumption, filter cake are taken out of and water loss) that system is discharged, namely after secondary sodium waste water drains into concentration basin, supernatant liquor is excessive in a large number, and system domestic demand discharges a large amount of waste water.
comparative example 2:
With comparative example 1 unlike, enter the supernatant liquor temperature about 30 DEG C (winter) of carbide-feed generator.
embodiment 1:
As shown in Figure 2, from the water of clean solution tank after interchanger regulating and controlling temperature, and calcium carbide adds in carbide-feed generator with set flow simultaneously, keeps the pressure and temperature of producer in set(ting)value, calcium carbide in producer and water react, and generate acetylene gas and carbide slag slurries; Acetylene gas from producer top successively through washing, compression after, enter acetylene cleaning post, with available chlorine be 0.1% ~ 0.12%, pH value be 7 ~ 8 fresh sodium solution remove the impurity such as hydrogen sulfide and phosphuret-(t)ed hydrogen in acetylene gas, secondary sodium waste water enters desorption one tower, spray under condition of negative pressure, after removing acetylene gas, a secondary sodium waste water part removes time sodium compositional apparatus, and another part enters concentration basin through aqueduct; Acetylene gas enters gas holder or next production process again after alkali cleaning, cooling; The carbide slag slurries overflowed from producer enters after desorption two tower reclaims acetylene gas in confined conditions, concentration basin is entered through aqueduct, supernatant liquor enters clean solution tank, and with after being pumped into aforesaid interchanger after water cooling tower cooling, temperature enters producer after being down to 25 DEG C.
Of the present invention time sodium compositional apparatus is two sections, and the first stage is: available chlorine is dense sodium solution of 10% and rawly disappears water with mass ratio 1:30 ~ 1:60 Homogeneous phase mixing in 1# Venturi reactor, obtains the centre time sodium solution of available chlorine 0.15% ~ 0.5%; Subordinate phase is: middle sodium solution and about 45% the secondary sodium waste water removing acetylene gas (available chlorine is 0.06%, the secondary sodium waste water of another 55% enters concentration basin through aqueduct) mix at 2# Venturi reactor, obtain and be used for fresh the sodium solution that peace and quiet available chlorine is 0.12%, the pH value of time sodium solution and useless time sodium solution in the middle of pH value on-line determination instrument by installing in second Venturi reactor measures, control by volume pump the amount adding acid, make the pH value of fresh chlorine bleach liquor 7 ~ 8.
The present invention reclaims on the acetylene pipeline of acetylene gas at desorption tower and is provided with online oxygen analyzer and Self controlling valve, energy on-line checkingi reclaims the content of oxygen in acetylene gas, and when oxygen content in acetylene gas is more than 1%, interlocking system starts, open blow-off valve, by emptying for the acetylene gas reclaimed.
The method of the present invention rate of recovery of dissolved acetylene in chlorine bleach liquor of giving up can reach more than 90%.
In method carbide slag slurries of the present invention, the rate of recovery of dissolved acetylene can reach more than 85%.
The process data of comparative example and embodiment is listed in table 1.
The parameter of table 1 comparative example and embodiment compares
Claims (8)
1. an acetylene production process for wastewater zero discharge, comprises following device:
(1) acetylene generator, calcium carbide and water generate thick acetylene gas in producer reaction;
(2) acetylene cleaning device, thick acetylene gas is after washing, peace and quiet with clorox (hereinafter referred to as secondary sodium) solution, to remove wherein a small amount of sulphur, phosphorus impurities, obtains highly purified acetylene gas for subsequent technique;
(3) useless time sodium reclaims acetylene and compositional apparatus, and the useless time sodium solution of peace and quiet generation enters desorption one tower, sprays under condition of negative pressure, and enter useless time sodium pond after reclaiming acetylene gas, a part removes time sodium compositional apparatus, and another part enters concentration basin through ramp pan;
(4) slag slurry reclaims acetylene unit, and the carbide slag slurries that producer produces enters desorption two tower in confined conditions, sprays, after removing acetylene gas wherein, enter concentration basin through ramp pan under condition of negative pressure;
(5) the concentrated filter-pressing device of slag slurry, after slag slurry is concentrated, clear liquid is back to use acetylene generator, and after the press filtration of dense slag slurry, filtrate returns concentration basin, and filter cake is as useless solid process.
2. the acetylene production process of a kind of wastewater zero discharge according to claim 1, is characterized in that: desorption one tower and desorption two tower share a set of negative pressure system.
3. useless time sodium according to claim 1 reclaims acetylene and compositional apparatus, it is characterized in that: useless time sodium solution enters desorption one tower and the acetylene desorption of dissolving reclaimed, and removes the useless time sodium solution acetylene content after acetylene lower than 100ppm.
4. according to claim 1,3, it is characterized in that: remove the useless chlorine bleach liquor's part after acetylene and go composite, part removes concentration basin through aqueduct, goes composite ratio about 20% ~ 80%.
5. the acetylene production process of a kind of wastewater zero discharge according to claim 1, is characterized in that: clear liquid, before entering producer, uses interchanger heat exchange, ensure that clear liquid enters the temperature-stable of producer, general between 15 ~ 35 DEG C, preferably 25 ~ 30 DEG C, optimum 25 DEG C.
6. the acetylene production process of a kind of wastewater zero discharge according to claim 2, is characterized in that: negative pressure device is made up of water ring vacuum pump and gas-liquid separator, vacuum tightness generally at 10kPa ~ 70kPa, preferred 40kPa ~ 70kPa.
7. useless time sodium according to claim 3 reclaims acetylene and compositional apparatus, it is characterized in that: secondary sodium solution compositional apparatus is primarily of two cover Venturi reactor compositions.
8. the acetylene production process of a kind of wastewater zero discharge according to claim 7, is characterized in that: be provided with pH value setting device at second Venturi reactor, by adding acid or alkali makes chlorine bleach liquor's pH value of preparation be 7 ~ 8.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410691882.0A CN105273760A (en) | 2014-11-27 | 2014-11-27 | Waste water zero-discharge acetylene production technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410691882.0A CN105273760A (en) | 2014-11-27 | 2014-11-27 | Waste water zero-discharge acetylene production technology |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105273760A true CN105273760A (en) | 2016-01-27 |
Family
ID=55143608
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410691882.0A Pending CN105273760A (en) | 2014-11-27 | 2014-11-27 | Waste water zero-discharge acetylene production technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105273760A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109663392A (en) * | 2019-02-14 | 2019-04-23 | 陕西金泰氯碱化工有限公司 | A kind of process that carbide slag slurries are separated by solid-liquid separation |
| CN111517525A (en) * | 2020-05-11 | 2020-08-11 | 北京中科众联新能源技术服务有限公司 | Process system and method for recycling acetylene and recycling water in waste sodium hypochlorite water |
| CN112374962A (en) * | 2020-10-13 | 2021-02-19 | 新疆中泰化学股份有限公司 | Method and device for efficiently applying low-mercury catalyst |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3829917B2 (en) * | 2001-05-28 | 2006-10-04 | 信越化学工業株式会社 | Acetylene production apparatus and production method thereof |
| CN101235319A (en) * | 2007-12-31 | 2008-08-06 | 常泽民 | Technique for extracting residual acetylene gas in acetylene generator (wet method) carbide slag slurry |
| CN101497549A (en) * | 2009-03-06 | 2009-08-05 | 河南神马氯碱化工股份有限公司 | Process for recycling sodium hypochlorite wastewater produced by purifying ethine |
| CN101575123A (en) * | 2008-05-11 | 2009-11-11 | 新疆天业（集团）有限公司 | Method for circularly preparing sodium hypochlorite solution by utilizing industrial wastewater containing sodium hypochlorite in acetylene production process |
| CN103664464A (en) * | 2013-12-03 | 2014-03-26 | 贵州开磷（集团）有限责任公司 | Method for recovering acetylene in waste sodium hypochlorite from acetylene purifying tower |
-
2014
- 2014-11-27 CN CN201410691882.0A patent/CN105273760A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3829917B2 (en) * | 2001-05-28 | 2006-10-04 | 信越化学工業株式会社 | Acetylene production apparatus and production method thereof |
| CN101235319A (en) * | 2007-12-31 | 2008-08-06 | 常泽民 | Technique for extracting residual acetylene gas in acetylene generator (wet method) carbide slag slurry |
| CN101575123A (en) * | 2008-05-11 | 2009-11-11 | 新疆天业（集团）有限公司 | Method for circularly preparing sodium hypochlorite solution by utilizing industrial wastewater containing sodium hypochlorite in acetylene production process |
| CN101497549A (en) * | 2009-03-06 | 2009-08-05 | 河南神马氯碱化工股份有限公司 | Process for recycling sodium hypochlorite wastewater produced by purifying ethine |
| CN103664464A (en) * | 2013-12-03 | 2014-03-26 | 贵州开磷（集团）有限责任公司 | Method for recovering acetylene in waste sodium hypochlorite from acetylene purifying tower |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109663392A (en) * | 2019-02-14 | 2019-04-23 | 陕西金泰氯碱化工有限公司 | A kind of process that carbide slag slurries are separated by solid-liquid separation |
| CN111517525A (en) * | 2020-05-11 | 2020-08-11 | 北京中科众联新能源技术服务有限公司 | Process system and method for recycling acetylene and recycling water in waste sodium hypochlorite water |
| CN112374962A (en) * | 2020-10-13 | 2021-02-19 | 新疆中泰化学股份有限公司 | Method and device for efficiently applying low-mercury catalyst |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105039989B (en) | A kind of acid chlorization system copper-containing etching waste solution electrodeposition decopper(ing) and regeneration method | |
| CN106399715A (en) | Method for producing electrolytic zinc through high-chloride zinc ash material ammonia leaching ion exchange combined process | |
| CN109665501A (en) | A kind of sulfate liquor fluorine circulation de-magging technique and system | |
| CN105951102A (en) | Method for reclamation of waste acid in hydrofluoric acid etching process | |
| CN105200248B (en) | A kind of step of utilization carbide slag one neutralizes the method that titanium white waste acid prepares high-purity scandium | |
| CN105273760A (en) | Waste water zero-discharge acetylene production technology | |
| CN106381397A (en) | Method for dechlorinating through zinc ash material ammonia-leaching ion exchange combined process | |
| CN106255666A (en) | The processing method of fluoride water and processing means | |
| CN103130369B (en) | Method of reusing sodium hypochlorite waste water generated by acetylene lustration | |
| CN1903750A (en) | Circulation reuse method of carbide slag supernatant fluid | |
| CN213446254U (en) | System for calcium sulfate is prepared and hydrochloric acid is retrieved to calcium chloride | |
| CN103723736A (en) | Resource recovery method in white carbon black production process | |
| CN104058539A (en) | Semi-fiber treatment process based on industrial waste water of viscose | |
| CN104876362A (en) | Acid purification recycling system | |
| CN218910533U (en) | Water electrolysis hydrogen production system | |
| CN108203083B (en) | Method and device for recovering waste sulfuric acid and waste aluminum sulfate during electrode foil production | |
| KR20180064753A (en) | Methods for waste water treatment of Nitrogen trifluoride(NF3) process | |
| CN107673539B (en) | Acidic wastewater treatment equipment and treatment method | |
| CN204162410U (en) | The harmless treatment unit of waste silicon powder | |
| CN109818099B (en) | Waste sulfuric acid recovery and regeneration system and method | |
| CN208562480U (en) | A kind of recovery system of cupric silicon powder | |
| CN202988883U (en) | Waste acid and waste saline water treatment system combining inorganic synthesis with reverse osmosis | |
| JP2011125812A (en) | Method for treating wastewater containing fluorine and silicon, method for producing calcium fluoride, and apparatus for treating fluorine-containing wastewater | |
| CN105905927B (en) | A kind of Galuber's salt type brine removes the bittern purifying device and method of strontium element | |
| CN220926685U (en) | Waste sodium hypochlorite recycling acetylene gas treatment system capable of recycling heat energy |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20160127 |