CN1035099A - Reclaim the method for prussiate - Google Patents
Reclaim the method for prussiate Download PDFInfo
- Publication number
- CN1035099A CN1035099A CN 87107312 CN87107312A CN1035099A CN 1035099 A CN1035099 A CN 1035099A CN 87107312 CN87107312 CN 87107312 CN 87107312 A CN87107312 A CN 87107312A CN 1035099 A CN1035099 A CN 1035099A
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- Prior art keywords
- decyanation
- cyanogen
- cyanide
- hcn
- prussiate
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- 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.)
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- Removal Of Specific Substances (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The present invention relates to a kind ofly contain the cyanogen trade effluent method that reclaims prussiate from lower concentration.Present method is with the cyanide wastewater recycle, make the cyanogen enrichment, extract a part of cyanide wastewater out, with stripping decyanation after the acidifying with pump, the HCN mixed gas that stripping comes out is removed moisture content and foreign gas through condensation separation, and gained liquid HCN and alkali or acetone reaction generate cyanide product.
It is big that present method is handled the water yield, can eliminate the pollution of prussiate to environment, can obtain the high cyanide product of purity again, remarkable in economical benefits, and environmental benefit is good.
Description
The present invention relates to a kind of method that from contain the cyanogen trade effluent, reclaims prussiate, be particularly useful for lower concentration and contain the cyanogen trade effluent, for example: ferromanganese blast furnace Coal-gas Washing Water Using and contain cyanogen ore dressing water.
At present, the method of handling industrial cyanide wastewater both at home and abroad is a lot, mainly contain pharmaceutical treatment and electrolytic process and atmospheric environment self-cleaning methods such as chlorinated lime, clorox, ozone, ferrous sulfate, sulfurous gas, these methods all are pure consumption-types, processing costs height not only, and in various degree secondary pollution is arranged.Have Shandong gold mine acidifying → blast aeration → NaOH similar with the present invention absorbs the production sodium cyanide method.This method working cost is higher, and processing cost and product income offsets substantially, simultaneously can not separating impurity gas, and product purity is unsecured.Also have coking final cold water to produce yellow prussiate of potash energy consumption height, the sales volume of the product is limited.
The objective of the invention is to enlarge the treatment capacity that contains the cyanogen trade effluent, the cyanide product that production purity is high is to obtain good benefits in environment and remarkable economic efficiency.
In order to achieve the above object, be subjected to the influence of pH value, promptly manyly under acidic conditions exist, manyly under alkaline condition exist with the salt state with the prussic acid molecularity according to the stability of prussiate in water, and the liquefying-point of prussic acid and CO
2, H
2The liquefying-point of S, HCl gas differs bigger characteristics, at first with the recycle under alkaline condition of lower concentration cyanide wastewater, make that prussiate is enriched to required concentration in the water, then, with pump extract out portion water with acidifying and preheating after, pump advances the decyanation tower, with the direct stripping decyanation of steam, the mixed gas that the decyanation tower comes out goes out HCN liquid through condensation separation, absorbs with absorption agents such as alkali and produces cyanide product.
Technical process of the present invention is as shown in Figure 1: the lower concentration cyanide wastewater of industrial discharge with alkaline matter control PH more than 8, after advancing settling tank precipitation and removing suspended substance, recycle, after treating that prussiate is enriched to finite concentration in the water, from circulating water pool, extract a part of water out with pump and regulate PH3-6 with acid to adding acid tank, the water yield of extracting out can be a principle at desirable value with the concentration that satisfies circulating water system cyanogen, water after the acidifying after interchanger heating with being pumped to the decyanation top of tower, in tower with the direct counter current contact decyanation of the steam of 2 kilograms of left and right sides pressure that enter at the bottom of the tower, waste water after the decyanation flows out from the tower bottom, flows back to circulating water pool after tower contains the heat exchange of cyanogen water at interchanger with advancing.The decyanation tower top temperature is controlled at 75～103 ℃, and HCN stripping in the waste water is gone out tower, and the mixed gas that comes out from the decyanation cat head is gone into tower through being cooled to 30～70 ℃ with most of steam condensing reflux.The high density HCN, the CO that come out from water cooler
2, H
2Mixed gass such as S enter condenser and are as cold as 0～20 ℃.Gas-liquid mixture is through separating CO
2, H
2Foreign gases such as S obtain liquid HCN.
As when adopting present method to produce NaCN or KCN, liquid HCN directly enters reactor and NaOH or KOH reaction generation NaCN or KCN.As producing acetone cyanohydrin, then HCN liquid enters the rectifying tower purification, reaches more than 99% for guaranteeing the HCN concentration that cat head comes out, and should control the rectifying tower top temperature is about 27 ℃.The HCN gas that rectifying tower top is come out is inflow reactor and acetone reaction generation acetone cyanohydrin after another condensation.
Carrying out the sodium cyanide product purity that medium-sized test produces with above-mentioned technology reaches more than 90%, no sulphur, no ammonia are measured through the chemical plant and Electroplate Factory tries out, and satisfy the industrial chemicals requirement fully, one ton of waste water that contains cyanogen 400～600mg/L of every processing, profitable more than 1.4 yuan.
Claims (6)
1, a kind ofly contain the cyanogen trade effluent method of receiving prussiate, it is characterized in that from lower concentration:
(1) lower concentration contains the cyanogen trade effluent at first through recycling concentration of cyanide.
(2) cyanide wastewater is directly used the steam decyanation in the decyanation tower after acidifying, and its decyanation rate reaches more than 98%.
(3) the HCN mixed gas that comes out from the decyanation tower cools off through the cat head water cooler and removes most water vapor.
(4) the HCN mixed gas that comes out from the cat head water cooler is removed foreign gas by condenser and gas-liquid separator.
2, by the method for claim 1, it is characterized in that: pH value is controlled at more than 8 in the recirculated water.
3, by the method for claim 1, it is characterized in that: advance decyanation tower cyanide wastewater pH value and be controlled at 3～6.
4, by the method for claim 1, it is characterized in that: the decyanation tower top temperature is controlled at 75～103 ℃.
5, by the method for claim 1, it is characterized in that: decyanation cat head chiller temperature is controlled at 30～70 ℃.
6, by the method for claim 1, it is characterized in that: temperature is controlled at 0～20 ℃ in the condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87107312 CN1012357B (en) | 1987-12-05 | 1987-12-05 | Method for recovery of cyanide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 87107312 CN1012357B (en) | 1987-12-05 | 1987-12-05 | Method for recovery of cyanide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1035099A true CN1035099A (en) | 1989-08-30 |
| CN1012357B CN1012357B (en) | 1991-04-17 |
Family
ID=4816045
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 87107312 Expired CN1012357B (en) | 1987-12-05 | 1987-12-05 | Method for recovery of cyanide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1012357B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102636616A (en) * | 2012-03-21 | 2012-08-15 | 云南昆钢煤焦化有限公司 | Method for testing content of hydrogen cyanide in gas |
| CN102701485A (en) * | 2012-06-19 | 2012-10-03 | 安徽朝山新材料股份有限公司 | Cyanide-containing wastewater treatment and recovery system |
| CN106335909A (en) * | 2016-10-20 | 2017-01-18 | 安庆市长虹化工有限公司 | Cyanide-containing wastewater recovery method and device |
| CN113045045A (en) * | 2021-03-26 | 2021-06-29 | 长春黄金研究院有限公司 | Complete device and method for treating acidified cyanide-containing wastewater by using atomized gas normal-temperature condensation method |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20150138210A (en) * | 2013-04-03 | 2015-12-09 | 다우 글로벌 테크놀로지스 엘엘씨 | Process for preparation of tertiary alkyl primary amines |
-
1987
- 1987-12-05 CN CN 87107312 patent/CN1012357B/en not_active Expired
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102636616A (en) * | 2012-03-21 | 2012-08-15 | 云南昆钢煤焦化有限公司 | Method for testing content of hydrogen cyanide in gas |
| CN102701485A (en) * | 2012-06-19 | 2012-10-03 | 安徽朝山新材料股份有限公司 | Cyanide-containing wastewater treatment and recovery system |
| CN106335909A (en) * | 2016-10-20 | 2017-01-18 | 安庆市长虹化工有限公司 | Cyanide-containing wastewater recovery method and device |
| CN113045045A (en) * | 2021-03-26 | 2021-06-29 | 长春黄金研究院有限公司 | Complete device and method for treating acidified cyanide-containing wastewater by using atomized gas normal-temperature condensation method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1012357B (en) | 1991-04-17 |
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