CN203990286U - A kind of processing is containing the CO 2 aerated device of cyanogen - Google Patents
A kind of processing is containing the CO 2 aerated device of cyanogen Download PDFInfo
- Publication number
- CN203990286U CN203990286U CN201420387221.4U CN201420387221U CN203990286U CN 203990286 U CN203990286 U CN 203990286U CN 201420387221 U CN201420387221 U CN 201420387221U CN 203990286 U CN203990286 U CN 203990286U
- Authority
- CN
- China
- Prior art keywords
- decyanation
- sections
- desulfurizing
- section
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn - After Issue
Links
Classifications
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Landscapes
- Industrial Gases (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a kind of device that contains cyanogen, carbon containing high concentration acid gas by naoh treatment, device comprises acid gas surge tank, decyanation decarbonization device, desulfurizer and product generating apparatus, decyanation decarbonization device comprises two sections of decyanation devices, and desulfurizer comprises three segments desulfurizing tower.Plant investment of the present utility model is few, floor space is little, absorption efficiency is high, three-waste free discharge; Use the utility model device first by the mode of the hydrogen cyanide of alkali absorption in advance, prevent that hydrogen cyanide from contacting with iron, thereby do not produce H2, in decyanization reaction, also can slough CO
2, i.e. decyanation simultaneously and decarburization.
Description
Technical field
The utility model relates to a kind of device of processing acid gas, is specifically related to a kind of device that contains cyanogen, carbon containing high concentration acid gas by naoh treatment, belonging to circulation and absorbing the high concentration acid gas technical field that Coal Chemical Industry extracting tower resolution gas forms.
Background technology
Mixed coal is in the process of heated coking, thereby coal gas is to be subject to high temperature action to make to obtain in the process of small molecule hydrocarbon class that the macromolecular cleavage of coal forms and hydrogen at mixed coal.Owing to inevitably can containing the elements such as carbon, nitrogen, sulphur, hydrogen in natural fossil fuel, in can being assigned to coal gas, go forming these elements in the process of coal gas, finally in coal gas with H
2s, CO
2, the form such as HCN exists.One of them factor that coke gas is different from other combustion gas is exactly that HCN and its esters all tool all have corrosivity to pipeline, and all have hypertoxicity because of the HCN that contains a great deal of.
The mode that HCN is processed in current domestic coal tar field has: 1, in desulfurization workshop section catalytic oxidation mode, hydrogen cyanide is changed into NH
4sCN or NaSCN, then extract these two kinds of salt.This method is a kind of both economical mode of processing desulfurization waste liquor, and NH
4sCN and the NaSCN market price are high, but the method is to conventional catalytic wet oxidation process matching, has reclaimed HCN, but by H
2s changes into low value (NH
4)
2sO
4, do not make economic interests reach maximization.2, by AS technique or Benfield technique, by more than 99% H in coal gas
2s, part CO
2, more than 99% HCN enters Analytic Tower after absorbing, then these three kinds of sour gas parsed, and produces sulphur or sulfuric acid.This method needs supporting claus oven or huge acid-making process, seriously polluted, complex operation, consumption of natural resource.3, at final cooling zone, gas temperature is reduced, the hydrogen cyanide gas in condensation coal gas, forms eventually cold waste water, the hydrogen cyanide in waste water is steamed out with steam, after heating, reacts yellow sodium prussiate processed with sodium carbonate liquor and iron filings.This method steam consumption quantity is large, loses more than gain, and application is restricted.4, combine with Fu Samu technique, after the absorbing ammonia of Fu Samu absorption tower containing cyanogen sulphur-containing gas, after heating, react yellow sodium prussiate processed with sodium carbonate and iron.This method is easily subject to the impact of other components in acid gas, and the secondary salt of generation is many, therefore just can produce waste liquid, needs extra process.
There are at present three kinds of methods to produce yellow sodium prussiate: sodium cyanide method, cyanide melt method and oven gas reclaim hydrogen cyanide method.Sodium cyanide method is to utilize Cymag and ferrous sulfate to mix directly and mix according to certain ratio, can directly obtain yellow sodium prussiate; This method is to produce at present the topmost method of yellow sodium prussiate.Cyanide melt method is that ferrous sulfate and cyanogas are mixed and produced in proportion; Although this method raw material is cheap, energy consumption is large, waste water is difficult.It is that the hydrogen cyanide steaming with steam and iron oxide and sodium carbonate mixing and contacting reaction are produced to yellow sodium prussiate that oven gas reclaims hydrogen cyanide method; This method must maintain 130 DEG C of above reaction temperatures, and purges cold waste water eventually and also need to consume a large amount of steam, and energy consumption is greatly the shortcoming of this kind of method.
Utility model content
For the technical problem of above-mentioned existence, the utility model provides a kind of processing containing the CO 2 aerated device of cyanogen, and this plant investment is few, floor space is little, absorption efficiency is high, yellow sodium prussiate quality is high, product NaHS concentration is adjustable, exhaust emissions is completely up to standard, three-waste free discharge can not cause secondary pollution, process not to produce H
2, economic worth is high.
The technical solution adopted in the utility model is:
A kind of processing is containing the CO 2 aerated device of cyanogen, described device comprises acid gas surge tank, decyanation decarbonization device, desulfurizer and product generating apparatus, described decyanation decarbonization device comprises one section of decyanation device, two sections of decyanation devices, one section of decyanation circulating pump and two sections of decyanation circulating pumps; Described desulfurizer comprises first grade desulfurizing heat exchanger, one section of desulfurizing tower, two-grade desulfurizing heat exchanger, two sections of desulfurizing towers, three grades of desulfurization heat exchangers, three grades of desulfurizing towers, one section of desulfuration recycle pump, two sections of desulfuration recycle pumps, three sections of desulfuration recycle pumps, NaHS medial launder, NaHS pump and concentration evaporators; Described product generating apparatus comprises yellow sodium prussiate medial launder, dissolves tower, dissolving circulation pump, lysate heater, separating tank, mother liquor tank, centrifuge and crystallization tank; Between described one section of decyanation device, two sections of decyanation devices, one section of desulfurizing tower, two sections of desulfurizing towers, three grades of desulfurizing towers, be communicated with successively; Described decyanation decarbonization device is connected with product generating apparatus by yellow sodium prussiate medial launder.
Described one section of desulfurizing tower, two sections of desulfurizing towers, three segments desulfurizing tower sides are respectively equipped with first grade desulfurizing heat exchanger, two-grade desulfurizing heat exchanger, three grades of desulfurization heat exchangers for cooling doctor solution.In described dissolving tower, be provided with iron plane flower fixed bed.Described separating tank position is than the high 0.5-2m in crystallization tank position.
The beneficial effects of the utility model are:
(1) plant investment of the present utility model is few, floor space is little, absorption efficiency is high, three-waste free discharge;
(2) using the product of the utility model device is adjustable 40% ~ 80% the NaHS aqueous solution or NaHS solid product and the purity yellow sodium prussiate solid 99% or more of purity more than 98% of solution concentration, and product economy is worth high;
(3) using the utility model installation method is by the mode of the hydrogen cyanide of alkali absorption in advance, prevents that hydrogen cyanide from contacting with iron, thereby does not produce H2, also can slough CO in decyanization reaction
2, i.e. decyanation simultaneously and decarburization;
(4) use the utility model installation method can remove more than 60% CO
2, removing more than 99.9% HCN and hydrogen sulfide, in tail gas, hydrogen sulfide content discharge value can be down to below 1mg/Nm3, completely qualified discharge.
Brief description of the drawings
Fig. 1 is the utility model process flow diagram;
In figure: 1 acid gas surge tank, 2 one sections of decyanation devices, 3 two sections of decyanation devices, 4 first grade desulfurizing heat exchangers, 5 one sections of desulfurizing towers, 6 two-grade desulfurizing heat exchangers, 7 two sections of desulfurizing towers, 8 three grades of desulfurization heat exchangers, 9 three grades of desulfurizing towers, 10 yellow sodium prussiate medial launders, 11 1 sections of decyanation circulating pumps, 12 2 sections of decyanation circulating pumps, 13 NaHS medial launders, 14 1 sections of desulfuration recycle pumps, 15 2 sections of desulfuration recycle pumps, 16 3 sections of desulfuration recycle pumps, 17 dissolve tower, 18 dissolving circulation pumps, 19 lysate heaters, 20 separating tanks, 21 mother liquor tanks, 22 centrifuges, 23 crystallization tanks, 24 NaHS pumps, 25 concentration evaporators.
Detailed description of the invention
Below the utility model is described in further detail.
As shown in Figure 1, a kind of processing is containing the CO 2 aerated device of cyanogen, described device comprises acid gas surge tank 1, decyanation decarbonization device, desulfurizer and product generating apparatus, described decyanation decarbonization device comprises one section of decyanation device 2, two sections of 3, one sections of decyanation circulating pumps 11 of decyanation device and two sections of decyanation circulating pumps 12; Described desulfurizer comprises first grade desulfurizing heat exchanger 4, one section of desulfurizing tower 5, two-grade desulfurizing heat exchanger 6, two sections of desulfurizing towers 7, three grades of desulfurization heat exchangers 8, three grades of desulfurizing towers 9, one section of desulfuration recycle pump 14, two sections of desulfuration recycle pumps 15, three sections of desulfuration recycle pumps 16, NaHS medial launder 13, NaHS pump 24 and concentration evaporators 25, and described one section of desulfurizing tower 5, two sections of desulfurizing towers 7, three segments desulfurizing tower 9 sides are respectively equipped with first grade desulfurizing heat exchanger 4, two-grade desulfurizing heat exchanger 6, three grades of desulfurization heat exchangers 8 for cooling doctor solution; Described product generating apparatus comprises yellow sodium prussiate medial launder 10, dissolves tower 17, dissolving circulation pump 18, lysate heater 19, separating tank 20, mother liquor tank 21, centrifuge 22 and crystallization tank 23, in described dissolving tower 17, be provided with iron plane flower fixed bed, described separating tank 20 positions are than the crystallization tank 23 high 1m in position; Between described one section of decyanation device 2, two sections of decyanation devices 3, one section of desulfurizing tower 5, two sections of desulfurizing towers 7, three grades of desulfurizing towers 9, be communicated with successively; Described decyanation decarbonization device is connected with product generating apparatus by yellow sodium prussiate medial launder 10.
Use device of the present utility model to process containing the CO 2 aerated method of cyanogen, comprise the following steps:
A, CO 2 aerated first by acid gas surge tank 1 containing cyanogen, then enter successively in one section of decyanation device 2 and two sections of decyanation devices 3 from one section of decyanation device 2 top, simultaneously continuous adds sodium hydroxide solution in two sections of decyanation devices 3, sodium hydroxide solution enters in two sections of decyanation devices 3 that contain excessive sodium hydrate after two sections of decyanation circulating pumps 12 stir together with acid gas, HCN, H in sodium hydroxide solution and acid gas
2s gas generation absorption reaction generates NaCN, Na
2s or NaHS, the reaction time is 15-60min, the solution reacting in rear two sections of decyanation devices 3 passes through after two sections of decyanation circulating pumps 12, then with enter one section of decyanation device 2 together with acid gas in, NaHS and CO
2there is row and analyse reaction generation NaHCO in gas
3and H
2s gas, the reaction time is 60-300min, row analyses reacted hydrogen sulfide and gets back in acid gas with the form of gas, the CO of absorption
2form with sodium acid carbonate exists, and the HCN of absorption exists with Cymag form, and mixed solution, as pretreated byproduct solution, completes decyanation decarbonizing process;
B, the acid gas of removing hydrogen cyanide and partial CO 2 enter in one section of desulfurizing tower 5, two sections of desulfurizing towers 7, three segments desulfurizing tower 9 successively, excessive sodium hydrate solution enters three segments desulfurizing tower 9, sodium hydroxide solution and H after three sections of desulfuration recycle pumps 16 stir together with acid gas simultaneously
2s gas generation absorption reaction generates Na
2s, the reaction time is 15-60min, reacted solution enters 7, two sections of interior solution of desulfurizing tower 7 of two sections of desulfurizing towers again and contains a large amount of Na together with acid gas
2s, sodium hydroxide solution and H
2s gas generation absorption reaction generates NaHS, and the reaction time is 15-60min, and reacted solution enters 5, one sections of interior solution of desulfurizing tower 5 of one section of desulfurizing tower again and contains a small amount of Na together with acid gas
2s, sodium hydroxide solution and H
2s gas generation absorption reaction generates NaHS, reaction time is 15-60min, reacted solution carries out concentration or dry processing after by one section of desulfuration recycle pump 14, makes sodium hydrosulfide or NaHS solid and enters NaHS medial launder 13, completes sweetening process;
C, the sodium hydroxide solution that reacts rear eliminating by one section of decyanation circulating pump 11 enters yellow sodium prussiate medial launder 10, after lysate heater 19 is heated to 170 DEG C, squeezes into and dissolve circulation sprinkling and iron plane flower fixed bed haptoreaction in tower 17 by dissolving circulation pump 18, after dissolving in tower iron plane flower in 17 and having dissolved, the separating tank 20 that is entered constant temperature by dissolving circulation pump 18 precipitates, after bulky grain precipitation in solution, clear liquid is entered to crystallization tank 23 use water quench to 50 DEG C, in crystallization tank 23, add yellow sodium prussiate crystal seed simultaneously, after the interior a large amount of crystal of groove 23 to be crystallized are separated out, crystal is put into the centrifugal yellow sodium prussiate solid that makes of centrifuge 22, complete the production of yellow sodium prussiate, clear liquid after centrifugal enters mother liquor tank 21, is drawn in two sections of decyanation devices 3 and is recycled by two sections of decyanation circulating pumps 12.
Described sodium hydroxide solution counter-current process is all to realize by level chain control.
Claims (4)
1. a processing is containing the CO 2 aerated device of cyanogen, it is characterized in that, described device comprises acid gas surge tank (1), decyanation decarbonization device, desulfurizer and product generating apparatus, described decyanation decarbonization device comprises one section of decyanation device (2), two sections of decyanation devices (3), one section of decyanation circulating pump (11) and two sections of decyanation circulating pumps (12); Described desulfurizer comprises first grade desulfurizing heat exchanger (4), one section of desulfurizing tower (5), two-grade desulfurizing heat exchanger (6), two sections of desulfurizing towers (7), three grades of desulfurization heat exchangers (8), three grades of desulfurizing towers (9), one section of desulfuration recycle pump (14), two sections of desulfuration recycle pumps (15), three sections of desulfuration recycle pumps (16), NaHS medial launder (13), NaHS pump (24) and concentration evaporator (25); Described product generating apparatus comprises yellow sodium prussiate medial launder (10), dissolves tower (17), dissolving circulation pump (18), lysate heater (19), separating tank (20), mother liquor tank (21), centrifuge (22) and crystallization tank (23); Between described one section of decyanation device (2), two sections of decyanation devices (3), one section of desulfurizing tower (5), two sections of desulfurizing towers (7), three grades of desulfurizing towers (9), be communicated with successively; Described decyanation decarbonization device is connected with product generating apparatus by yellow sodium prussiate medial launder (10).
2. processing according to claim 1 is containing the CO 2 aerated device of cyanogen, it is characterized in that, described one section of desulfurizing tower (5), two sections of desulfurizing towers (7), three segments desulfurizing tower (9) side are respectively equipped with first grade desulfurizing heat exchanger (4), two-grade desulfurizing heat exchanger (6), three grades of desulfurization heat exchangers (8) for cooling doctor solution.
3. processing according to claim 1, containing the CO 2 aerated device of cyanogen, is characterized in that, is provided with iron plane flower fixed bed in described dissolving tower (17).
4. processing according to claim 1, containing the CO 2 aerated device of cyanogen, is characterized in that, described separating tank (20) position is than crystallization tank (23) the high 0.5-2m in position.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420387221.4U CN203990286U (en) | 2014-07-15 | 2014-07-15 | A kind of processing is containing the CO 2 aerated device of cyanogen |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420387221.4U CN203990286U (en) | 2014-07-15 | 2014-07-15 | A kind of processing is containing the CO 2 aerated device of cyanogen |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203990286U true CN203990286U (en) | 2014-12-10 |
Family
ID=52030359
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420387221.4U Withdrawn - After Issue CN203990286U (en) | 2014-07-15 | 2014-07-15 | A kind of processing is containing the CO 2 aerated device of cyanogen |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203990286U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104069730A (en) * | 2014-07-15 | 2014-10-01 | 袁磊 | Device and method for treating cyanogen-containing and carbon-containing acid gas |
| CN110216135A (en) * | 2019-07-16 | 2019-09-10 | 科盛环保科技股份有限公司 | A kind of multistage decyanation tower of cyanamide waste residue |
-
2014
- 2014-07-15 CN CN201420387221.4U patent/CN203990286U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104069730A (en) * | 2014-07-15 | 2014-10-01 | 袁磊 | Device and method for treating cyanogen-containing and carbon-containing acid gas |
| CN104069730B (en) * | 2014-07-15 | 2015-10-21 | 袁磊 | A kind of process contains the CO 2 aerated device and method of cyanogen |
| CN110216135A (en) * | 2019-07-16 | 2019-09-10 | 科盛环保科技股份有限公司 | A kind of multistage decyanation tower of cyanamide waste residue |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101333464B (en) | Desulphurization process by vacuum ammonia method | |
| CN106673014B (en) | Process for preparing ammonia water by desulfurization and deamination of coke oven gas | |
| CN108998106B (en) | Desulfurization and deamination method for coking plant | |
| CN103693626B (en) | A kind ofly carbonated hydrogen sulfide acid gas is utilized to prepare the method for Sodium sulfhydrate | |
| CN103011201B (en) | Method for extracting ammonium thiocyanate from ammonia-process desulfurization waste liquid by oxidation process | |
| CN102061197B (en) | Coke oven gas desulfuration and deamination combined purifying method and special device thereof | |
| CN103418223A (en) | Comprehensive desulphurization technology in coal chemical industry | |
| CN105036438A (en) | Harmless treatment method for sodium alkali desulfurization waste solution | |
| CN201658945U (en) | Sintering smoke purifying system based on heat pipe afterheat recovery technology | |
| CN103570046B (en) | Process for preparing high-purity sodium sulfite through sulfuric acid production industrial exhaust | |
| CN101457162A (en) | Wet-type absorption coke oven gas desulphurization and decyanation process using ammine as alkali source | |
| CN104628012A (en) | Production method for preparing ammonium sulfate by alkylating waste acid | |
| CN105505480A (en) | Desulfurization purification system applicable to coke oven gas | |
| CN104986817A (en) | Method for treating sewage containing sulfur and ammonia during alternation working procedure of synthetic ammonia by using steam stripping method | |
| CN203990286U (en) | A kind of processing is containing the CO 2 aerated device of cyanogen | |
| CN105441140A (en) | Coke oven gas purifying system | |
| CN203033778U (en) | Device for producing ammonium sulfate by using sulfate pulp and ammonia water as raw materials | |
| CN109517630B (en) | Process and system for deamination production of ammonium sulfate by coke oven gas ammonium sulfite method | |
| CN209702677U (en) | Coke-stove gas sulfurous acid ammonium salt process deamination produces sulphur ammonium system | |
| CN105642090B (en) | A kind of Acidic Gas Treating method and device | |
| CN104069730B (en) | A kind of process contains the CO 2 aerated device and method of cyanogen | |
| CN113150837B (en) | Coke oven gas desulfurization process | |
| CN103351891B (en) | New process for carrying out desulfurization, decyanation and decarbonization by using sodium hydroxide and separating reaction products | |
| CN204601970U (en) | A kind of device reduced discharging for the fuming furnace sulfur-containing tail gas degree of depth | |
| CN105694988A (en) | Process for solving coal gas desulfuration liquid expansion in coking industry and system for process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20141210 Effective date of abandoning: 20151021 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |