CN102502707B - Method for purifying hydrocyanic acid from mixed gas containing hydrocyanic acid - Google Patents
Method for purifying hydrocyanic acid from mixed gas containing hydrocyanic acid Download PDFInfo
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- CN102502707B CN102502707B CN201110329027.1A CN201110329027A CN102502707B CN 102502707 B CN102502707 B CN 102502707B CN 201110329027 A CN201110329027 A CN 201110329027A CN 102502707 B CN102502707 B CN 102502707B
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Abstract
The invention discloses a method for purifying hydrocyanic acid from mixed gas containing the hydrocyanic acid, which comprises an absorption step and a rectification step, wherein in the absorption step, pressurizing the mixed gas containing the hydrocyanic acid to 0.11-1.5 MPa, then cooling to 10-80 DEG C, introducing into a pressure absorption tower, and pressurizing and absorbing the hydrocyanic acid in the mixed gas with absorption liquid, i.e. acidic aqueous solution with a pH value of 1-6 under the conditions that the pressure in the tower is 0.11-1.0 MPa, and the temperature is 0-60 DEG C to obtain hydrocyanic acid absorption liquid. The method has the beneficial effects that the existing atmospheric absorption method is replaced by a pressure absorption method to absorb the hydrocyanic acid in the mixed gas containing the hydrocyanic acid; the absorption temperature can be improved to 60 DEG C; the concentration of the hydrocyanic acid in the hydrocyanic acid absorption liquid can be improved by 3-10 times, so that the purifying efficiency of the hydrocyanic acid can be remarkably improved; and meanwhile, the energy consumption is greatly reduced and can be reduced by 80 percent to a maximum extent.
Description
Technical field
The invention belongs to chemical field, relate to a kind of from produce the reaction mixture gas of prussic acid the method for purifying hydrocyanic acid.
Background technology
Prussic acid is a kind of broad-spectrum industrial chemicals, can be applicable to the various fields such as medicine, agricultural chemicals, makeup, dyestuff, chemical fertilizer, plating, polymer, photograph, mining industry, metallurgy.The production method of prussic acid mainly contains iS-One method (Andrussow method), BMA method, light oil cracking method, vinyl cyanide by-product method etc.IS-One method is to pass into oxidation reactor after methane, ammonia and oxygen are fully mixed by a certain percentage, and take platinum rhodium or platinum iridium alloy as catalyzer, under normal pressure, more than 1000 ℃ condition, prussic acid is synthesized in reaction.BMA method is the improvement to iS-One method, does not need oxygen to participate in reaction, is take platinum as catalyzer, and the reaction under normal pressure, more than 1300 ℃ condition of methane and ammonia is synthesized to prussic acid.Light oil cracking method is take light oil (or gasoline), liquefied ammonia and caustic soda as main raw material, refinery coke grain and nitrogen are the working system of auxiliary material, first make light oil and liquid ammonia gasification, and in spraying gun, mix in proportion, be preheated to 280 ℃, by three-phase electrode, immerse the boiling reaction stove of refinery coke granulosa conductive exothermal, under normal pressure, 1450 ℃ of conditions, can be cleaved into the splitting gas containing 20 ~ 25% prussic acid.Vinyl cyanide by-product method is that this method is take propylene, ammonia and air in petroleum gas as raw material by the method for propylene ammmoxidation process acrylonitrile production coproduct hydrogen cyanic acid, and propylene and ammonia mix by a certain percentage sends into oxidation reactor, by sparger, is evenly spread in beds; Air enters from reactor bottom by a certain percentage, through grid distributor, upwards flows, and mixes and make catalyst bed laminarization with propylene, ammonia; Reactant generates vinyl cyanide under 440 ~ 450 ℃ and catalyst action, simultaneously coproduct hydrogen cyanic acid.The reaction mixture gas that adopts iS-One method, BMA method or light oil cracking method production prussic acid to obtain need, through except ammonia, absorption, rectifying three step process, could obtain highly purified liquid hydrogen cyanic acid.Wherein, except ammonia step is to remove the unreacted raw material ammonia completely containing in reaction mixture gas; Absorption step is with acid absorption liquid, under condition of normal pressure, to absorb the hydrocyanic acid gas containing except in gas mixture after ammonia, obtains prussic acid absorption liquid; Rectification step is that prussic acid absorption liquid is carried out to atmospheric distillation, collects prussic acid cut, obtains liquid hydrogen cyanic acid after condensation.Adopt the prussic acid gas mixture that contains that vinyl cyanide by-product method makes not need except ammonia, through absorption, rectifying two step process, just can obtain highly purified liquid hydrogen cyanic acid.But in above-mentioned prussic acid purifying technique, absorption step not only requires lower absorption temperature (10 ~ 15 ℃), the energy consumption of needs of causing lowering the temperature is high, and the prussic acid concentration in gained prussic acid absorption liquid lower (being about 10g/L), causes prussic acid purification efficiency low.
Summary of the invention
In view of this, the object of the present invention is to provide a kind ofly from the method containing purifying hydrocyanic acid prussic acid gas mixture, do not need lower absorption temperature, and in gained prussic acid absorption liquid, the concentration of prussic acid is higher, thereby can significantly improve the purification efficiency of prussic acid, greatly reduce energy consumption simultaneously.
For achieving the above object, the invention provides following technical scheme:
From the method containing purifying hydrocyanic acid prussic acid gas mixture, comprise absorption step and rectification step, described absorption step is to be forced into 0.11 ~ 1.5MPa containing prussic acid gas mixture, be cooled to again 10 ~ 80 ℃, pass into pressurizing absorption tower, in tower internal pressure, being that 0.11 ~ 1.0MPa, temperature are under the condition of 0 ~ 60 ℃, is that pH is the hydrocyanic acid gas in 1 ~ 6 acidic aqueous solution pressurizing absorption gas mixture with absorption liquid, obtains prussic acid absorption liquid.Described acidic aqueous solution can be both the inorganic aqueous acids such as sulfuric acid, hydrochloric acid, phosphoric acid, can be also the organic acid aqueous solution such as acetic acid, oxalic acid, the preferably sulfuric acid aqueous solution.
Because gas compression meeting causes gas temperature to rise, (gas compression is than larger, gas temperature raises more), hypertonia will increase the energy consumption of compression and cooling, prussic acid belongs to hypertoxic class material, high pressure will increase facility investment and security risk greatly, and the easy polymerization of prussic acid under hot conditions and affect product yield, therefore, absorption step select suitable absorption pressure and absorption temperature extremely important.Preferably, described absorption step is to be forced into 0.2 ~ 0.7MPa containing prussic acid gas mixture, be cooled to again 30 ~ 50 ℃, pass into pressurizing absorption tower, in tower internal pressure, be that 0.15 ~ 0.6Mpa, temperature are under the condition of 20 ~ 40 ℃, hydrocyanic acid gas in the acidic aqueous solution pressurizing absorption gas mixture that is 2 ~ 5 with pH, obtains prussic acid absorption liquid.Preferred, described absorption step is to be forced into 0.7MPa containing prussic acid gas mixture, be cooled to again 45 ℃, pass into pressurizing absorption tower, in tower internal pressure, be that 0.3 ~ 0.5Mpa, temperature are under the condition of 25 ~ 30 ℃, hydrocyanic acid gas in the aqueous sulfuric acid pressurizing absorption gas mixture that is 2 with pH, obtains prussic acid absorption liquid.
For better utilised system thermal and improve the rate of recovery of prussic acid, preferably, the distillation residual liquid of described prussic acid absorption liquid and rectification step gained carries out sending into rectifying tower after heat exchange and carries out rectifying, and distillation residual liquid returns to absorption step as absorption liquid recycled through heat exchange and after being cooled to absorption temperature.
Rectification step of the present invention can be both atmospheric distillation, can be also rectification under vacuum, and concrete technology condition can be determined according to the boiling point of water and prussic acid.Wherein, atmospheric distillation is preferably that 90 ~ 120 ℃, tower top temperature are to carry out under the condition of 15 ~ 40 ℃ in tower reactor temperature, in tower reactor temperature, is more preferably that 100 ~ 110 ℃, tower top temperature are to carry out under the condition of 20 ~ 30 ℃; Rectification under vacuum is preferably that 60 ~ 80 ℃, tower top temperature are to carry out under the condition of 0 ~ 15 ℃ in tower reactor temperature.Rectification under vacuum can reduce the service temperature of rectifying tower, makes absorption more approaching with the service temperature of rectifying, further reduces production energy consumption.
Above-mentioned prussic acid method of purification is applicable to all prussic acid production methods in industrial application at present, such as iS-One method, BMA method, light oil cracking method, vinyl cyanide by-product method etc., be specially adapted to purifying hydrocyanic acid from the reaction mixture gas of the synthetic prussic acid of iS-One method.
From the reaction mixture gas of the synthetic prussic acid of iS-One method, BMA method or light oil cracking method during purifying hydrocyanic acid, before absorption step, also comprise except ammonia step, described except ammonia step be to remove the unreacted raw material ammonia completely containing in reaction mixture gas, to prevent that this part ammonia from causing polymerization, the decomposition of prussic acid in subsequent processes.Ammonia-removal method both can adopt sulfuric acid process, utilized sulfuric acid absorption ammonia to generate sulphur ammonium; Also can adopt phosphorus ammonium method, its principle is to absorb at low temperatures the ammonia in gas mixture with phosphorus ammonium barren liquor (NH3/H3PO4 mol ratio is 1.1 ~ 1.4), generate diammonium phosphate and emit heat, the phosphorus ammonium barren liquor that has absorbed ammonia becomes phosphorus ammonium pregnant liquor (mol ratio of NH3/H3PO4 is 1.7 ~ 1.9), under hot conditions, desorb is decomposed again, emits ammonia and absorbs heat, changes phosphorus ammonium barren liquor into and recycles after cooling, the ammonia that desorb is emitted obtains ammoniacal liquor through condensation, and ammoniacal liquor obtains liquefied ammonia through rectifying.
Beneficial effect of the present invention is: the present invention adopts pressurizing absorption method to substitute existing normal pressure absorption process in absorption step, 1. in prussic acid absorption liquid, the concentration of prussic acid can improve 3 ~ 10 times, when the prussic acid absorption liquid of follow-up rectifying same volume, can once obtain the more liquid hydrogen cyanic acid of volume, thereby greatly improve prussic acid purification efficiency; 2. absorption temperature can be increased to 60 ℃, does not need reaction mixture gas to be cooled to lesser temps (10 ~ 15 ℃) again, thereby greatly reduces cooling energy consumption; 3. the prussic acid absorption liquid that pressurizing absorption makes is with certain pressure, variation due to pressure when it enters normal pressure or rectification under vacuum tower can flash distillation steam part hydrocyanic acid gas, and, because the concentration of prussic acid in gained prussic acid absorption liquid improves, obtain the rectifying time shorten that equivalent liquid hydrogen cyanic acid needs, thereby greatly reduce rectifying energy consumption; 4. distillation residual liquid can return to absorption step as absorption liquid recycled through heat exchange and after being further cooled to absorption temperature, because absorption temperature obviously improves, distillation residual liquid is cooled to the needed energy consumption of absorption temperature and also significantly reduces; Comprehensive above-mentioned several aspects, through engineering calculation and experimental verification, adopt the inventive method, and production energy consumption is the highest declines 80%.
Accompanying drawing explanation
Fig. 1 is from the device schematic diagram containing purifying hydrocyanic acid prussic acid gas mixture, and wherein 1 for removing ammoniacal liquor test tank, and 2 for removing ammonia tower, 3 for removing ammoniacal liquor water cooler, and 4 for removing the cooling device of ammonia gas mixture, and 5 is compressor, 6 is the cooling device of pressurization gas mixture, and 7 is pressurization gas mixture surge tank, and 8 is pressurizing absorption tower, 9 is interchanger, 10 is atmospheric distillation tower, and 11 is rectifying reboiler, and 12 is prussic acid condenser, 13 is prussic acid receiving tank, and 14 is distillation residual liquid water cooler.
Embodiment
In order to make the object, technical solutions and advantages of the present invention clearer, below in conjunction with accompanying drawing, the preferred embodiments of the present invention are described in detail.
embodiment 1, from the reaction mixture gas of the synthetic prussic acid of iS-One method purifying hydrocyanic acid
Device schematic diagram as shown in Figure 1.
A. except ammonia: to adding except ammoniacal liquor (aqueous sulfuric acid that pH is 4) except in ammoniacal liquor test tank 1, the reaction mixture gas of the synthetic prussic acid of iS-One method is passed into except ammonia tower 2 by bottom, simultaneously from spraying into except ammoniacal liquor except ammonia tower 2 tops, reaction mixture gas is through removing after the ammonia wherein containing except ammoniacal liquor counter-current absorption, from removing ammonia tower 2 tops out, through being cooled to 40 ℃ except the cooling device 4 of ammonia gas mixture; The ammoniacal liquor that removes after absorbing ammonia recycles after cooling except ammoniacal liquor water cooler 3, regularly replaces the new ammoniacal liquor that removes;
B. absorb: will with compressor 5, be forced into 0.7MPa except the reaction mixture gas after ammonia, then be cooled to 45 ℃ through the cooling device 6 of pressurization gas mixture, pass into pressurization gas mixture surge tank 7; Pressurization gas mixture in pressurization gas mixture surge tank 7 is passed into pressurizing absorption tower 8 with constant pressure 0.7MPa by bottom, from the top of pressurizing absorption tower 8, spray into absorption liquid (aqueous sulfuric acid that pH is 2) simultaneously, control tower internal pressure is that 0.4MPa, temperature are 30 ℃, hydrocyanic acid gas in absorption liquid counter-current absorption pressurization gas mixture, the prussic acid absorption liquid that acquisition concentration is 68g/L;
C. rectifying: the prussic acid absorption liquid flowing out from pressurizing absorption tower 8 bottoms and the distillation residual liquid flowing out from atmospheric distillation tower 10 bottoms are undertaken heat exchange by interchanger 9, by middle part, pass into atmospheric distillation tower 10, flash distillation steams part hydrocyanic acid gas, remaining liq carries out atmospheric distillation after rectifying reboiler 11 heating at the bottom of tower, controlling tower reactor temperature is 110 ℃, dephlegmator of top of the tower temperature is 28 ℃, from atmospheric distillation tower 10 tops gas out after prussic acid condenser 12 cooling, send into prussic acid receiving tank 13, obtain the liquid hydrogen cyanic acid of high purity (quality percentage composition >=99%), the distillation residual liquid (prussic acid that contains quality percentage composition < 0.01%) flowing out from atmospheric distillation tower 10 bottoms is undertaken heat exchange by interchanger 9 with the prussic acid absorption liquid flowing out from pressurizing absorption tower 8 bottoms, through distillation residual liquid water cooler 14, be cooled to 25 ℃, return to pressurizing absorption tower 8 as absorption liquid recycled.
embodiment 2, from the reaction mixture gas of the synthetic prussic acid of iS-One method purifying hydrocyanic acid
The difference of the present embodiment and embodiment 1 is:
In absorption step, the pressure of controlling pressurizing absorption tower 8 is that 0.3MPa, temperature are 25 ℃, and finally obtaining concentration is the prussic acid absorption liquid of 52g/L.
embodiment 3, from the reaction mixture gas of the synthetic prussic acid of iS-One method purifying hydrocyanic acid
The difference of the present embodiment and embodiment 1 is:
In absorption step, the pressure of controlling pressurizing absorption tower 8 is that 0.5MPa, temperature are 28 ℃, and finally obtaining concentration is the prussic acid absorption liquid of 72g/L.
embodiment 4, from the reaction mixture gas of the synthetic prussic acid of iS-One method purifying hydrocyanic acid
The difference of the present embodiment and embodiment 1 is:
Absorption step is to be forced into 0.11MPa except the reaction mixture gas compressor 5 after ammonia, then is cooled to 10 ℃ through the cooling device 6 of pressurization gas mixture, passes into pressurization gas mixture surge tank 7; Pressurization gas mixture in pressurization gas mixture surge tank 7 is passed into pressurizing absorption tower 8 with constant pressure 0.11MPa by bottom, from pressurizing absorption tower 8 tops, spray into absorption liquid (aqueous hydrochloric acid that pH is 1) simultaneously, control tower internal pressure is that 0.11MPa, temperature are 0 ℃, hydrocyanic acid gas in absorption liquid counter-current absorption pressurization gas mixture, the prussic acid absorption liquid that acquisition concentration is 25g/L;
Rectification step is to be 90 ℃ in tower reactor temperature, and dephlegmator of top of the tower temperature is to carry out atmospheric distillation under the condition of 15 ℃; Distillation residual liquid returns to pressurizing absorption tower 8 as absorption liquid recycled through heat exchange and after being further cooled to 0 ℃.
embodiment 5, from the reaction mixture gas of the synthetic prussic acid of iS-One method purifying hydrocyanic acid
The difference of the present embodiment and embodiment 1 is:
Absorption step is to be forced into 0.2MPa except the reaction mixture gas compressor 5 after ammonia, then is cooled to 30 ℃ through the cooling device 6 of pressurization gas mixture, passes into pressurization gas mixture surge tank 7; Pressurization gas mixture in pressurization gas mixture surge tank 7 is passed into pressurizing absorption tower 8 with constant pressure 0.2MPa by bottom, from pressurizing absorption tower 8 tops, spray into absorption liquid (phosphate aqueous solution that pH is 3) simultaneously, control tower internal pressure is that 0.15MPa, temperature are 20 ℃, hydrocyanic acid gas in absorption liquid counter-current absorption pressurization gas mixture, the prussic acid absorption liquid that acquisition concentration is 43g/L;
Rectification step is to be 100 ℃ in tower reactor temperature, and dephlegmator of top of the tower temperature is to carry out atmospheric distillation under the condition of 20 ℃; Distillation residual liquid returns to pressurizing absorption tower 8 as absorption liquid recycled through heat exchange and after being further cooled to 20 ℃.
embodiment 6, from the reaction mixture gas of the synthetic prussic acid of iS-One method purifying hydrocyanic acid
The difference of the present embodiment and embodiment 1 is:
Absorption step is to be forced into 0.6MPa except the reaction mixture gas compressor 5 after ammonia, then is cooled to 50 ℃ through the cooling device 6 of pressurization gas mixture, passes into pressurization gas mixture surge tank 7; Pressurization gas mixture in pressurization gas mixture surge tank 7 is passed into pressurizing absorption tower 8 with constant pressure 0.6MPa by bottom, from pressurizing absorption tower 8 tops, spray into absorption liquid (acetic acid aqueous solution that pH is 5) simultaneously, control tower internal pressure is that 0.6MPa, temperature are 40 ℃, hydrocyanic acid gas in absorption liquid counter-current absorption pressurization gas mixture, the prussic acid absorption liquid that acquisition concentration is 45g/L;
Rectification step is to be 105 ℃ in tower reactor temperature, and dephlegmator of top of the tower temperature is to carry out atmospheric distillation under the condition of 30 ℃; Distillation residual liquid returns to pressurizing absorption tower 8 as absorption liquid recycled through heat exchange and after being further cooled to 30 ℃.
embodiment 7, from the reaction mixture gas of the synthetic prussic acid of iS-One method purifying hydrocyanic acid
The difference of the present embodiment and embodiment 1 is:
Absorption step is to be forced into 1.5MPa except the reaction mixture gas compressor 5 after ammonia, then is cooled to 60 ℃ through the cooling device 6 of pressurization gas mixture, passes into pressurization gas mixture surge tank 7; Pressurization gas mixture in pressurization gas mixture surge tank 7 is passed into pressurizing absorption tower 8 with constant pressure 1.5MPa by bottom, from pressurizing absorption tower 8 tops, spray into absorption liquid (oxalic acid aqueous solution that pH is 6) simultaneously, control tower internal pressure is that 1.0MPa, temperature are 60 ℃, hydrocyanic acid gas in absorption liquid counter-current absorption pressurization gas mixture, the prussic acid absorption liquid that acquisition concentration is 38g/L;
Rectification step is to be 120 ℃ in tower reactor temperature, and dephlegmator of top of the tower temperature is to carry out atmospheric distillation under the condition of 40 ℃; Distillation residual liquid returns to pressurizing absorption tower 8 as absorption liquid recycled through heat exchange and after being further cooled to 60 ℃.
embodiment 8, from the reaction mixture gas of the synthetic prussic acid of iS-One method purifying hydrocyanic acid
A. except ammonia: identical with embodiment 1;
B. absorb: will with compressor 5, be forced into 0.5MPa except the reaction mixture gas after ammonia, then be cooled to 40 ℃ through the cooling device 6 of pressurization gas mixture, pass into pressurization gas mixture surge tank 7; Pressurization gas mixture in pressurization gas mixture surge tank 7 is passed into pressurizing absorption tower 8 with constant pressure 0.5MPa by bottom, from pressurizing absorption tower 8 tops, spray into absorption liquid (acetic acid aqueous solution that pH is 5) simultaneously, control tower internal pressure is that 0.4MPa, temperature are 30 ℃, hydrocyanic acid gas in absorption liquid counter-current absorption pressurization gas mixture, the prussic acid absorption liquid that acquisition concentration is 45g/L;
C. rectifying: the prussic acid absorption liquid flowing out from pressurizing absorption tower bottom and the distillation residual liquid flowing out from rectification under vacuum tower bottom are undertaken heat exchange by interchanger, by middle part, pass into rectification under vacuum tower, flash distillation steams part hydrocyanic acid gas, remaining liq carries out rectification under vacuum after the rectifying reboiler heating at the bottom of tower, controlling tower reactor temperature is 75 ℃, dephlegmator of top of the tower temperature is 10 ℃, from rectification under vacuum top of tower gas out, after the cooling of prussic acid condenser, send into prussic acid receiving tank, obtain the liquid hydrogen cyanic acid of high purity (quality percentage composition >=99%); The distillation residual liquid (prussic acid that contains quality percentage composition < 0.01%) flowing out from rectification under vacuum tower bottom is undertaken heat exchange by interchanger with the prussic acid absorption liquid flowing out from pressurizing absorption tower bottom, through distillation residual liquid water cooler, be cooled to 30 ℃, return to pressurizing absorption tower as absorption liquid recycled.
embodiment 9, from the reaction mixture gas of the synthetic prussic acid of light oil cracking method purifying hydrocyanic acid
The difference of the present embodiment and embodiment 1 is:
Except in ammonia step, the reaction mixture gas of the synthetic prussic acid of light oil cracking method is passed into except ammonia tower 2 by bottom, simultaneously from spraying into except ammoniacal liquor except ammonia tower 2 tops, reaction mixture gas is through removing after the ammonia wherein containing except ammoniacal liquor counter-current absorption, from removing ammonia tower 2 tops out, through being cooled to 40 ℃ except the cooling device 4 of ammonia gas mixture.
embodiment 10, from light oil cracking legal system for purifying hydrocyanic acid prussic acid gas mixture
The difference of the present embodiment and embodiment 9 is:
Rectification step is that the prussic acid absorption liquid flowing out from pressurizing absorption tower bottom and the distillation residual liquid flowing out from rectification under vacuum tower bottom are undertaken heat exchange by interchanger, by middle part, pass into rectification under vacuum tower, flash distillation steams part hydrocyanic acid gas, remaining liq carries out rectification under vacuum after the rectifying reboiler heating at the bottom of tower, controlling tower reactor temperature is 73 ℃, dephlegmator of top of the tower temperature is 15 ℃, from rectification under vacuum top of tower gas out, after the cooling of prussic acid condenser, send into prussic acid receiving tank, obtain the liquid hydrogen cyanic acid of high purity (quality percentage composition >=99%); The distillation residual liquid (prussic acid that contains quality percentage composition < 0.01%) flowing out from rectification under vacuum tower bottom is undertaken heat exchange by interchanger with the prussic acid absorption liquid flowing out from pressurizing absorption tower bottom, through distillation residual liquid water cooler, be cooled to 25 ℃, return to pressurizing absorption tower as absorption liquid recycled.
embodiment 11, from vinyl cyanide by-product method gained containing purifying hydrocyanic acid prussic acid gas mixture
A. absorb: will with compressor 5, be forced into 1.5MPa except the prussic acid gas mixture after ammonia, then be cooled to 80 ℃ through the cooling device 6 of pressurization gas mixture, pass into pressurization gas mixture surge tank 7; Pressurization gas mixture in pressurization gas mixture surge tank 7 is passed into pressurizing absorption tower 8 with constant pressure 1.5MPa by bottom, from pressurizing absorption tower 8 tops, spray into absorption liquid (oxalic acid aqueous solution that pH is 6) simultaneously, control tower internal pressure is that 1.0MPa, temperature are 60 ℃, hydrocyanic acid gas in absorption liquid counter-current absorption pressurization gas mixture, the prussic acid absorption liquid that acquisition concentration is 48g/L;
B. rectifying: the prussic acid absorption liquid flowing out from pressurizing absorption tower 8 bottoms and the distillation residual liquid flowing out from atmospheric distillation tower 10 bottoms are undertaken heat exchange by interchanger 9, by middle part, pass into atmospheric distillation tower 10, flash distillation steams part hydrocyanic acid gas, remaining liq carries out atmospheric distillation after rectifying reboiler 11 heating at the bottom of tower, controlling tower reactor temperature is 120 ℃, dephlegmator of top of the tower temperature is 40 ℃, from atmospheric distillation tower 10 tops gas out after prussic acid condenser 12 cooling, send into prussic acid receiving tank 13, obtain the liquid hydrogen cyanic acid of high purity (quality percentage composition >=99%), the distillation residual liquid (prussic acid that contains quality percentage composition < 0.01%) flowing out from atmospheric distillation tower 10 bottoms is undertaken heat exchange by interchanger 9 with the prussic acid absorption liquid flowing out from pressurizing absorption tower 8 bottoms, through distillation residual liquid water cooler 14, be cooled to 60 ℃, return to pressurizing absorption tower 8 as absorption liquid recycled.
embodiment 12, from vinyl cyanide by-product method gained containing purifying hydrocyanic acid prussic acid gas mixture
The difference of the present embodiment and embodiment 11 is:
Rectification step is that the prussic acid absorption liquid flowing out from pressurizing absorption tower bottom and the distillation residual liquid flowing out from rectification under vacuum tower bottom are undertaken heat exchange by interchanger, by middle part, pass into rectification under vacuum tower, flash distillation steams part hydrocyanic acid gas, remaining liq carries out rectification under vacuum after the rectifying reboiler heating at the bottom of tower, controlling tower reactor temperature is 60 ℃, dephlegmator of top of the tower temperature is 0 ℃, from rectification under vacuum top of tower gas out, after the cooling of prussic acid condenser, send into prussic acid receiving tank, obtain the liquid hydrogen cyanic acid of high purity (quality percentage composition >=99%); The distillation residual liquid (prussic acid that contains quality percentage composition < 0.01%) flowing out from rectification under vacuum tower bottom is undertaken heat exchange by interchanger with the prussic acid absorption liquid flowing out from pressurizing absorption tower bottom, through distillation residual liquid water cooler, be cooled to 60 ℃, return to pressurizing absorption tower as absorption liquid recycled.
Finally explanation is, above embodiment is only unrestricted in order to technical scheme of the present invention to be described, although by with reference to the preferred embodiments of the present invention, invention has been described, but those of ordinary skill in the art is to be understood that, can to it, make various changes in the form and details, and not depart from the spirit and scope of the present invention that appended claims limits.
Claims (3)
1. from the method containing purifying hydrocyanic acid prussic acid gas mixture, comprise absorption step and rectification step, it is characterized in that: described absorption step is to be forced into 0.7MPa containing prussic acid gas mixture, be cooled to again 45 ℃, pass into pressurizing absorption tower, in tower internal pressure, be that 0.3 ~ 0.5Mpa, temperature are under the condition of 25 ~ 30 ℃, the hydrocyanic acid gas in the aqueous sulfuric acid pressurizing absorption gas mixture that is 2 with pH, obtains prussic acid absorption liquid; The distillation residual liquid of described prussic acid absorption liquid and rectification step gained carries out sending into rectifying tower after heat exchange and carries out rectifying, and distillation residual liquid returns to absorption step as absorption liquid recycled through heat exchange and after being cooled to absorption temperature.
2. according to claim 1 from the method containing purifying hydrocyanic acid prussic acid gas mixture, it is characterized in that: described is to adopt iS-One method, BMA method or light oil cracking method to produce the reaction mixture gas that prussic acid obtains containing prussic acid gas mixture, and by removing ammonia step, has removed the ammonia containing in reaction mixture gas before absorption step.
3. according to claim 1 from the method containing purifying hydrocyanic acid prussic acid gas mixture, it is characterized in that: described is the reaction mixture gas containing prussic acid that adopts vinyl cyanide by-product method to make containing prussic acid gas mixture.
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| CN101218177A (en) * | 2005-06-07 | 2008-07-09 | 巴斯福股份公司 | Process for preparing salts of hydrocyanic acid |
| CN101264901A (en) * | 2008-04-29 | 2008-09-17 | 石家庄工大化工设备有限公司 | Ammonia recovery method for gas mixture in hydrogen cyanide production |
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| JPS57129822A (en) * | 1981-02-05 | 1982-08-12 | Asahi Chem Ind Co Ltd | Recovering and purifying method for hydrocyanic acid |
| CN1055917C (en) * | 1997-06-06 | 2000-08-30 | 中国石油化工总公司 | Acrylonitrile absorbing tower |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US2899274A (en) * | 1956-12-31 | 1959-08-11 | Recovery of ammonia and hydrogen | |
| CN1217324A (en) * | 1997-11-13 | 1999-05-26 | 中国石油化工总公司 | Process for recovering and refining olefinic nitrile |
| CN1413977A (en) * | 2001-10-22 | 2003-04-30 | 中国石油化工股份有限公司 | Acrylonitrile fluidized-bed catalyst |
| CN101218177A (en) * | 2005-06-07 | 2008-07-09 | 巴斯福股份公司 | Process for preparing salts of hydrocyanic acid |
| CN101264901A (en) * | 2008-04-29 | 2008-09-17 | 石家庄工大化工设备有限公司 | Ammonia recovery method for gas mixture in hydrogen cyanide production |
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