CN204237574U - Prussic acid purifying and liquefying also utilizes the device producing sodium cyanide containing cyanogen combined tail gas - Google Patents
Prussic acid purifying and liquefying also utilizes the device producing sodium cyanide containing cyanogen combined tail gas Download PDFInfo
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- CN204237574U CN204237574U CN201420704135.1U CN201420704135U CN204237574U CN 204237574 U CN204237574 U CN 204237574U CN 201420704135 U CN201420704135 U CN 201420704135U CN 204237574 U CN204237574 U CN 204237574U
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- sodium cyanide
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- prussic acid
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- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 title claims abstract description 193
- KXZJHVJKXJLBKO-UHFFFAOYSA-N chembl1408157 Chemical compound N=1C2=CC=CC=C2C(C(=O)O)=CC=1C1=CC=C(O)C=C1 KXZJHVJKXJLBKO-UHFFFAOYSA-N 0.000 title claims abstract description 69
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 title claims 20
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 90
- 239000007788 liquid Substances 0.000 claims abstract description 76
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 48
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 33
- 238000010521 absorption reaction Methods 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000003860 storage Methods 0.000 claims abstract description 20
- 239000007921 spray Substances 0.000 claims abstract description 19
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 13
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 13
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 13
- 230000009615 deamination Effects 0.000 claims abstract description 3
- 238000006481 deamination reaction Methods 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 45
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- XLJMAIOERFSOGZ-UHFFFAOYSA-N cyanic acid Chemical compound OC#N XLJMAIOERFSOGZ-UHFFFAOYSA-N 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 8
- 238000012856 packing Methods 0.000 claims description 7
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims 4
- 229910052739 hydrogen Inorganic materials 0.000 claims 4
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 4
- 238000007664 blowing Methods 0.000 claims 2
- 239000012530 fluid Substances 0.000 claims 1
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 abstract description 5
- 230000018044 dehydration Effects 0.000 abstract description 5
- 238000006297 dehydration reaction Methods 0.000 abstract description 5
- 238000009833 condensation Methods 0.000 abstract description 3
- 230000005494 condensation Effects 0.000 abstract description 3
- 230000015572 biosynthetic process Effects 0.000 description 9
- 238000003786 synthesis reaction Methods 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000007864 aqueous solution Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 238000007255 decyanation reaction Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000003513 alkali Substances 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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Abstract
一种氢氰酸提纯液化并利用含氰尾气联合生产氰化钠的装置，包括依次连接的除氨塔、氢氰酸预冷器、汽水分离器、氢氰酸脱水器，氢氰酸冷凝器、液体氢氰酸收集罐、氰化钠吸收塔；除氨塔的排液口经阀门二、脱氨液冷却器与脱氨液循环泵相连，脱氨液循环泵的出口端分别与除氨塔、硫酸铵贮槽相连；汽水分离器底部排液管与除氨塔相连接；硫酸经氢氰酸脱水器与除氨塔相连；液碱经氰化钠喷淋转料泵与氰化钠吸收塔相连，氰化钠吸收塔经氰化钠喷淋转料泵与氰化钠产品贮槽相连。本实用新型通过脱氨、预冷却、脱水、冷凝凝液化获取液体氢氰酸并用含氰尾气联合生产氰化钠。
A device for purifying and liquefying hydrocyanic acid and using cyanide-containing tail gas to jointly produce sodium cyanide, including a sequentially connected ammonia removal tower, hydrocyanic acid precooler, steam-water separator, hydrocyanic acid dehydrator, and hydrocyanic acid condenser , liquid hydrocyanic acid collection tank, sodium cyanide absorption tower; the discharge port of the ammonia removal tower is connected with the ammonia removal liquid circulation pump through the valve two, the ammonia removal liquid cooler, and the outlet end of the ammonia removal liquid circulation pump is connected with the ammonia removal liquid circulation pump respectively. Tower and ammonium sulfate storage tank are connected; the drain pipe at the bottom of the steam-water separator is connected with the ammonia removal tower; the sulfuric acid is connected with the ammonia removal tower through a hydrocyanic acid dehydrator; The absorption tower is connected, and the sodium cyanide absorption tower is connected with the sodium cyanide product storage tank through the sodium cyanide spray transfer pump. The utility model obtains liquid hydrocyanic acid through deamination, precooling, dehydration, condensation and liquefaction, and uses cyanide-containing tail gas to jointly produce sodium cyanide.
Description
技术领域 technical field
本实用新型涉及一种氢氰酸提纯液化并利用含氰尾气联合生产氰化钠的装置。 The utility model relates to a device for purifying and liquefying hydrocyanic acid and utilizing tail gas containing cyanide to jointly produce sodium cyanide.
背景技术 Background technique
现有的氢氰酸提纯液化装置采用氢氰酸合成气经过吸收塔低温水吸收，然后加热解析精馏获取含量达99%以上的液体氢氰酸。这不仅仅要求将吸收氢氰酸的水冷冻至较低的温度，导致降低温度需要能耗高，并且所得的氢氰酸吸收液中氢氰酸的浓度较低（约为10~20g/L），导致氢氰酸提纯效率低，为了将溶于水中的氢氰酸蒸出，需要进行精馏、再冷凝，才能得到高纯度的液体氢氰酸，用吸收精馏的方法每生产一吨氢氰酸，消耗蒸汽高达15吨。此外，传统的氢氰酸吸收精馏工艺，是不可能完全将氢氰酸的气体吸收，因此，在吸收后的尾气中会夹带少量的氢氰酸，这些夹带的氢氰酸随尾气的焚烧而损失掉，没能得到充分利用。 The existing hydrogen cyanide purification and liquefaction device adopts hydrogen cyanide synthesis gas to absorb through the low-temperature water of the absorption tower, and then heats, analyzes and rectifies to obtain liquid hydrogen cyanide with a content of more than 99%. This not only requires the water that absorbs prussic acid to be frozen to a lower temperature, which leads to high energy consumption for lowering the temperature, but also has a low concentration of prussic acid in the resulting prussic acid absorption solution (about 10 ~ 20g/L ), leading to low purification efficiency of hydrocyanic acid. In order to distill the hydrocyanic acid dissolved in water, rectification and recondensation are required to obtain high-purity liquid hydrocyanic acid. Hydrocyanic acid consumes up to 15 tons of steam. In addition, the traditional hydrocyanic acid absorption rectification process is impossible to completely absorb the gas of hydrocyanic acid. Therefore, a small amount of hydrocyanic acid will be entrained in the exhaust gas after absorption. And lost, not fully utilized.
发明内容 Contents of the invention
本实用新型提供一种氢氰酸提纯液化并利用含氰尾气联合生产氰化钠的装置，利用化学吸收不可逆的特点，解决了现有技术生产氢氰酸消耗能源高、氢氰酸利用率较低的不足，提高了氢氰酸的综合利用率，且生产过程安全环保。 The utility model provides a device for purifying and liquefying hydrocyanic acid and using cyanide-containing tail gas to jointly produce sodium cyanide. By utilizing the irreversible characteristics of chemical absorption, it solves the problems of high energy consumption and relatively low utilization rate of hydrocyanic acid in the production of hydrocyanic acid in the prior art. The low deficiency improves the comprehensive utilization rate of hydrocyanic acid, and the production process is safe and environment-friendly.
本实用新型的技术方案是：包括除氨塔、与除氨塔的塔顶出气口相连的氢氰酸预冷器、与氢氰酸预冷器出口相连的汽水分离器、与汽水分离器顶部气体出口相连的氢氰酸脱水器，与氢氰酸脱水器顶部气体出口相连的氢氰酸冷凝器、与氢氰酸冷凝器出口相连的液体氢氰酸收集罐、与液体氢氰酸收集罐顶部尾气出口相连的氰化钠吸收塔；除氨塔塔顶内设液体分布器一，塔顶出气口处设尾气排气管，除氨塔内装规整填料，除氨塔的排液口经阀门二、脱氨液冷却器与脱氨液循环泵相连，脱氨液循环泵的出口端分别与除氨塔塔顶内装的液体分布器一、硫酸铵贮槽相连； 汽水分离器底部排液管与除氨塔相连接；硫酸经氢氰酸脱水器与除氨塔相连；加一次酸解决了两个设备上对酸的需求。脱水器利用的是硫酸的脱水能力，除氨塔利用的是硫酸的酸性来吸收碱性的氨。氰化钠吸收塔塔顶内设液体分布器二，塔顶端设尾气排气管，氰化钠吸收塔内装规整填料，液碱经氰化钠喷淋转料泵与氰化钠吸收塔塔顶内装的液体分布器二相连，氰化钠吸收塔塔釜釜底设料液管道，料液管道经氰化钠喷淋转料泵与氰化钠产品贮槽相连。 The technical scheme of the utility model is: including the ammonia removal tower, the hydrocyanic acid precooler connected with the outlet of the tower top of the ammonia removal tower, the steam-water separator connected with the outlet of the hydrogen cyanide precooler, and the top of the steam-water separator The hydrocyanic acid dehydrator connected to the gas outlet, the hydrocyanic acid condenser connected to the gas outlet on the top of the hydrocyanic acid dehydrator, the liquid hydrocyanic acid collection tank connected to the hydrocyanic acid condenser outlet, and the liquid hydrocyanic acid collection tank The sodium cyanide absorption tower connected to the tail gas outlet at the top; a liquid distributor 1 is installed in the top of the ammonia removal tower, and a tail gas exhaust pipe is installed at the gas outlet on the top of the tower; structured packing is installed in the ammonia removal tower; 2. The deammonization liquid cooler is connected with the deammonization liquid circulation pump, and the outlet end of the deammonization liquid circulation pump is respectively connected with the liquid distributor 1 and the ammonium sulfate storage tank installed in the top of the ammonia removal tower; the bottom drain pipe of the steam-water separator It is connected with the ammonia removal tower; the sulfuric acid is connected with the ammonia removal tower through the hydrocyanic acid dehydrator; the addition of acid solves the demand for acid on the two devices. The dehydrator uses the dehydration ability of sulfuric acid, and the ammonia removal tower uses the acidity of sulfuric acid to absorb alkaline ammonia. The top of the sodium cyanide absorption tower is equipped with a liquid distributor 2, and the top of the tower is equipped with a tail gas exhaust pipe. The sodium cyanide absorption tower is equipped with regular packing. The built-in liquid distributors are connected to each other, and the bottom of the sodium cyanide absorption tower tank is equipped with a feed liquid pipeline, which is connected to the sodium cyanide product storage tank through the sodium cyanide spray transfer pump.
所述脱氨液循环泵的出口端分别经阀门与液体分布器一、硫酸铵贮槽相连。 The outlet end of the deammonization liquid circulating pump is respectively connected with the liquid distributor 1 and the ammonium sulfate storage tank through valves.
所述汽水分离器底部排液管上设有阀门三。 The drain pipe at the bottom of the steam-water separator is provided with a valve three.
所述硫酸经管道、阀门四与氢氰酸脱水器相连，氢氰酸脱水器的排液管经阀门五与除氨塔相连。 The sulfuric acid is connected to the hydrocyanic acid dehydrator through pipeline and valve four, and the drain pipe of the hydrocyanic acid dehydrator is connected to the ammonia removal tower through valve five.
所述液体氢氰酸收集罐底部设氢氰酸放料管道，氢氰酸放料管道设有阀门六，液体氢氰酸收集罐顶部尾气出口经阀门七与氰化钠吸收塔相连。 The bottom of the liquid hydrocyanic acid collection tank is provided with a hydrocyanic acid discharge pipeline, and the hydrocyanic acid discharge pipeline is provided with a valve six, and the tail gas outlet on the top of the liquid hydrocyanic acid collection tank is connected to the sodium cyanide absorption tower through a valve seven.
所述液碱经管道、装于管道上的阀门八与氰化钠喷淋转料泵进口端相连。 The liquid caustic soda is connected to the inlet end of the sodium cyanide spray transfer pump through the pipeline and the valve eight installed on the pipeline.
所述氰化钠吸收塔的料液管道上设有阀门九，氰化钠吸收塔的料液管道经阀门九与氰化钠喷淋转料泵进口端相连。 The feed liquid pipeline of the sodium cyanide absorption tower is provided with a valve nine, and the feed liquid pipeline of the sodium cyanide absorption tower is connected to the inlet end of the sodium cyanide spray transfer pump through the valve nine.
所述氰化钠喷淋转料泵的出口端经阀门十与液体分布器二相连，氰化钠喷淋转料泵的出口端经阀门十一与氰化钠产品贮槽相连。 The outlet end of the sodium cyanide spray transfer pump is connected to the liquid distributor two through the valve ten, and the outlet end of the sodium cyanide spray transfer pump is connected to the sodium cyanide product storage tank through the valve eleven.
所述氰化钠产品贮槽顶部设有进料口，氰化钠喷淋转料泵的出口端经阀门十一与氰化钠产品贮槽的进料口相连。 The top of the sodium cyanide product storage tank is provided with a feed inlet, and the outlet end of the sodium cyanide spray transfer pump is connected to the feed inlet of the sodium cyanide product storage tank through valve eleven.
与现有技术相比，本实用新型涉及一种通过脱氨、预冷却、脱水、冷凝凝液化获取液体氢氰酸并用含氰尾气联合生产氰化钠的装置。本实用新型在提纯和液化氢氰酸时不需要蒸汽，降低了生产氢氰酸的能耗，同时尾气采用串联的碱吸收塔使少量的氢氰酸气完全吸收，提高了氢氰酸的综合利用率，且生产过程安全环保。 Compared with the prior art, the utility model relates to a device for obtaining liquid hydrocyanic acid through deamination, precooling, dehydration, condensation and liquefaction, and using cyanide-containing tail gas to jointly produce sodium cyanide. The utility model does not need steam when purifying and liquefying hydrocyanic acid, which reduces the energy consumption of producing hydrocyanic acid. At the same time, a small amount of hydrocyanic acid gas is completely absorbed by a series of alkali absorption towers for the tail gas, which improves the synthesis of hydrocyanic acid. utilization rate, and the production process is safe and environmentally friendly.
附图说明 Description of drawings
图1为本实用新型的结构示意图。 Fig. 1 is the structural representation of the utility model.
具体实施方式 Detailed ways
除氨塔1塔顶内设液体分布器，塔顶端设尾气排气管，塔体内装规整填料。 氢氰酸合成气除氨塔1与氢氰酸合成气来源管道相连，管道设阀门控制开关及进气流量调节。除氨塔1的塔顶出气口用管道与氢氰酸预冷器2相连接，氢氰酸预冷器2出口与汽水分离器3用管道相连接。汽水分离器3上端设气体管道与氢氰酸脱水器4相连，底部设排液管道与除氨塔1的塔釜相连接，管路上设阀门控制开关。氢氰酸脱水器4顶部气体出口与氢氰酸冷凝器5 间用管道相连接，设硫酸进料管道与脱水器顶端相连，管道上设阀门控制开关。脱水器4底部设排液管道，该管道与汽水分离器3底部排液管并管后与除氨塔1相连接，并管前设阀门以便控制开关。氢氰酸冷凝器5通过管道与液体氢氰酸收集罐6顶部进料口相连接。液体氢氰酸收集罐6顶部设尾气出口管与氰化钠吸收塔相连接，管道上设阀门控制，收集罐6底部设氢氰酸放料管道并设阀门控制开关，根据生产需要将液体氢氰酸引向氢氰酸使用系统。 A liquid distributor is arranged on the top of the ammonia removal tower 1, and a tail gas exhaust pipe is arranged on the top of the tower, and structured packing is installed in the tower. Hydrocyanic acid synthesis gas ammonia removal tower 1 is connected to the source pipeline of hydrogen cyanide synthesis gas, and the pipeline is equipped with valve control switch and intake flow adjustment. The gas outlet at the top of the ammonia removal tower 1 is connected with the hydrocyanic acid precooler 2 with a pipeline, and the 2 outlets of the hydrocyanic acid precooler are connected with the steam-water separator 3 with a pipeline. The upper end of the steam-water separator 3 is provided with a gas pipeline connected to the hydrocyanic acid dehydrator 4, and the bottom is provided with a liquid discharge pipeline connected with the reactor of the ammonia removal tower 1, and a valve control switch is provided on the pipeline. The gas outlet at the top of the hydrocyanic acid dehydrator 4 is connected to the hydrocyanic acid condenser 5 with pipes, the sulfuric acid feed pipe is connected to the top of the dehydrator, and the valve control switch is arranged on the pipe. A drain pipe is arranged at the bottom of the dehydrator 4, which is connected with the drain pipe at the bottom of the steam-water separator 3 and then connected with the ammonia removal tower 1, and a valve is arranged in front of the pipe so as to control the switch. Hydrocyanic acid condenser 5 is connected with liquid hydrocyanic acid collection tank 6 top feeding ports by pipeline. The top of the liquid hydrocyanic acid collection tank 6 is provided with a tail gas outlet pipe connected to the sodium cyanide absorption tower, the pipeline is provided with valve control, and the bottom of the collection tank 6 is provided with a hydrocyanic acid discharge pipe and a valve control switch. The cyanic acid leads to the hydrocyanic acid using system.
氰化钠吸收塔7塔顶内设液体分布器，塔顶端设尾气排气管，塔体内装规整填料。塔釜釜底设料液管道与料液泵8的进口端相连，管道上设阀门控制开关，料液泵8的出口分两路管线，一路管道接氰化钠吸收塔7的塔顶液体分布器，在连接液体分布器前设有阀门控制开关，另一路管道连接氰化钠产品贮槽9顶部进料口，在连接进料口前设有阀门控制开关，以上两路管道根据需要实行一开一闭。 A liquid distributor is arranged on the top of the sodium cyanide absorption tower 7, and a tail gas exhaust pipe is arranged on the top of the tower, and structured packing is installed in the tower. The feed liquid pipeline at the bottom of the tower kettle is connected to the inlet end of the feed liquid pump 8, and a valve control switch is arranged on the pipeline. The outlet of the feed liquid pump 8 is divided into two pipelines, and one pipeline is connected to the top liquid distribution of the sodium cyanide absorption tower 7 A valve control switch is provided before connecting the liquid distributor, and another pipeline is connected to the feed inlet at the top of the sodium cyanide product storage tank 9, and a valve control switch is provided before connecting the feed inlet, and the above two pipelines are implemented as required. Open and close.
除氨塔1底部排液口设管道与脱氨液冷却器10进口端相连，管道上设阀门控制开关。脱氨液冷却器10的出口段与脱氨液循环泵11的进口端相连。脱氨液循环泵11的出口端分为两路管道，一路管道连接除氨塔1塔顶内装的液体分布器，在连接液体分布器前设有阀门控制开关；另一路管道连接硫酸铵贮槽12顶部进料口，在连接进料口前设有阀门控制开关，以上两路管道根据需要实行一开一闭。 The liquid outlet at the bottom of the ammonia removal tower 1 is provided with a pipeline connected to the inlet of the deammonization liquid cooler 10, and a valve control switch is provided on the pipeline. The outlet section of the deammonized liquid cooler 10 is connected to the inlet end of the deammonized liquid circulating pump 11 . The outlet end of the deammonization liquid circulation pump 11 is divided into two pipelines, one pipeline is connected to the liquid distributor built in the top of the ammonia removal tower 1, and a valve control switch is arranged before connecting the liquid distributor; the other pipeline is connected to the ammonium sulfate storage tank 12 The top feeding port is equipped with a valve control switch before connecting the feeding port, and the above two pipelines are opened and closed as required.
具体过程如下： The specific process is as follows:
1、生产准备： 1. Production preparation:
通过管道将70%的硫酸转入氢氰酸脱水器4。在运转期间通过部分排除吸水后被稀释的硫酸（脱水后浓度降低的硫酸用来脱氨），补加商品化的98%的浓硫酸实现循环。 70% sulfuric acid is transferred to hydrocyanic acid dehydrator 4 by pipeline. During operation, the sulfuric acid diluted after absorbing water is partially removed (the sulfuric acid with reduced concentration after dehydration is used for deammonization), and commercial 98% concentrated sulfuric acid is added to realize circulation.
通过氢氰酸脱水器4的排液管将适量的硫酸溶液放入除氨塔1，循环润湿除氨塔内填料。 Put an appropriate amount of sulfuric acid solution into the ammonia removal tower 1 through the drain pipe of the hydrocyanic acid dehydrator 4, and circulate and wet the packing in the ammonia removal tower.
通过氰化钠喷淋转料泵8将商品化的液碱转入氰化钠吸收塔7，循环润湿氰化钠吸收塔塔内填料。 The commercialized liquid caustic soda is transferred to the sodium cyanide absorption tower 7 through the sodium cyanide spray transfer pump 8, and the filler in the sodium cyanide absorption tower is circulated and wetted.
2、生产过程 2. Production process
氢氰酸合成气通过管道从除氨塔1的下部进入，通过气体阀门调解进气流量大小，气体自下而上逆流上升。通过脱氨循液环泵11将含有硫酸的脱氨液，脱氨液是循环中的硫酸水溶液，在循环过程中形成的是硫酸、硫酸氢铵、硫酸铵中一种活几种的混合物。通过除氨塔1塔顶的液体分布器在塔内均匀喷淋分散。在塔釜收集液体后依靠脱氨液循环泵11实现循环，同时用脱氨液冷却器10控制脱氨液温度，使氢氰酸合成气中残留的氨得以完全吸收，定期将硫酸铵吸收液用循环泵转入硫酸铵贮槽12。除氨后的合成气通过管道进入氢氰酸预冷器2，预冷器2把经过氨吸收液带入的水份冷凝形成氢氰酸水溶液进入汽水分离器3，收集的氢氰酸水溶液通过管道进入除氨塔闭路循环脱氰，即汽水分离器的氢氰酸水溶液在回到除氨塔中，受热分离出氢氰酸气体，使塔顶氢氰酸富集。脱氰后水从硫酸铵溶液中带走。直到形成全系统的气液相平衡。冷凝脱水后的氢氰酸合成气通过管道进入氢氰酸脱水器4。 Hydrocyanic acid synthesis gas enters from the lower part of the ammonia removal tower 1 through a pipeline, and the gas valve adjusts the intake flow rate, and the gas rises countercurrently from bottom to top. The deammonization liquid containing sulfuric acid is passed through the deammonization circulating liquid circulation pump 11, and the deammonization liquid is a sulfuric acid aqueous solution in the circulation, and what is formed in the circulation process is a mixture of sulfuric acid, ammonium bisulfate, and ammonium sulfate. Evenly spray and disperse in the tower through the liquid distributor at the top of the ammonia removal tower 1. After collecting the liquid in the tower kettle, rely on the deammonization liquid circulating pump 11 to realize circulation, and simultaneously use the deammonization liquid cooler 10 to control the deammonization liquid temperature, so that the residual ammonia in the prussic acid synthesis gas can be completely absorbed, and the ammonium sulfate absorption liquid is regularly absorbed Transfer to ammonium sulfate storage tank 12 with circulation pump. The synthesis gas after ammonia removal enters the hydrocyanic acid precooler 2 through the pipeline, and the precooler 2 condenses the water brought in by the ammonia absorption liquid to form a hydrocyanic acid aqueous solution and enters the steam-water separator 3, and the collected hydrocyanic acid aqueous solution passes through The pipeline enters the ammonia removal tower for closed-circuit decyanation, that is, the hydrocyanic acid aqueous solution in the steam-water separator is returned to the ammonia removal tower, and the hydrogen cyanide gas is separated by heating to enrich the hydrogen cyanide at the top of the tower. Water is carried away from the ammonium sulfate solution after decyanation. Until the gas-liquid phase equilibrium of the whole system is formed. The hydrocyanic acid synthesis gas after the condensation dehydration enters the hydrocyanic acid dehydrator 4 through the pipeline.
在这里用60%~70%浓度的硫酸充分脱去残留的水份，脱水后的氢氰酸合成气经过气体管道进入氢氰酸冷凝器5，在氢氰酸冷凝器5中充分冷凝液化，得到含量达到99.5%以上、水份控制在0.1%以内的液化的氢氰酸，贮存在液体氢氰酸收集罐6内，供生产中使用。部分没有液化的氢氰酸随着尾气通过管道进入氰化钠吸收塔7。用氰化钠喷淋转料泵8将塔内的氢氧化钠水溶液喷淋循环吸收尾气中残留的氢氰酸，形成氰化钠溶液，在含量符合要求时通过关闭氰化钠喷淋吸收循环管道阀，打开氰化钠贮槽转料管道阀门，将氰化钠水溶液转入氰化钠贮槽9。 Here, sulfuric acid with a concentration of 60%~70% is used to fully remove the remaining water, and the dehydrated hydrocyanic acid synthesis gas enters the hydrocyanic acid condenser 5 through the gas pipeline, and is fully condensed and liquefied in the hydrocyanic acid condenser 5. Obtain the liquefied hydrocyanic acid whose content reaches more than 99.5% and the moisture content is controlled within 0.1%, and store it in the liquid hydrocyanic acid collection tank 6 for use in production. Part of the hydrocyanic acid that is not liquefied enters the sodium cyanide absorption tower 7 through the pipeline along with the tail gas. Use sodium cyanide spray transfer pump 8 to spray and circulate the sodium hydroxide aqueous solution in the tower to absorb the residual hydrocyanic acid in the tail gas to form a sodium cyanide solution. When the content meets the requirements, close the sodium cyanide spray absorption cycle Pipeline valve, open sodium cyanide storage tank material transfer pipeline valve, sodium cyanide aqueous solution is transferred to sodium cyanide storage tank 9.
除氨塔1中的除氨液在硫酸铵浓度达到预设指标后，通过脱氨液循环泵部分转入硫酸铵贮槽，用于后续工序生产硫酸铵。 After the ammonium sulfate concentration reaches the preset target, the ammonia removal liquid in the ammonia removal tower 1 is partially transferred to the ammonium sulfate storage tank through the deammonization liquid circulation pump, and is used for the production of ammonium sulfate in the subsequent process.
Claims (9)
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107750235A (en) * | 2015-06-18 | 2018-03-02 | Epc工程与技术有限公司 | Prepare the effective ways of the removing toxic substances of the waste gas and waste water containing cyanide in the method for alkali metal cyanide |
| CN111362279A (en) * | 2020-04-23 | 2020-07-03 | 营口德瑞化工有限公司 | System and method for continuously producing sodium thiocyanate-free and by-producing ammonium sulfate from cracking furnace gas |
-
2014
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107750235A (en) * | 2015-06-18 | 2018-03-02 | Epc工程与技术有限公司 | Prepare the effective ways of the removing toxic substances of the waste gas and waste water containing cyanide in the method for alkali metal cyanide |
| CN107750235B (en) * | 2015-06-18 | 2021-03-19 | Epc工程与技术有限公司 | Effective method for detoxification of cyanide-containing waste gas and waste water in the method for preparing alkali metal cyanide |
| US11905179B2 (en) | 2015-06-18 | 2024-02-20 | Cyplus Gmbh | Efficient method for decontaminating waste gases and waste water containing cyanide in a method for producing alkali metal cyanides |
| CN111362279A (en) * | 2020-04-23 | 2020-07-03 | 营口德瑞化工有限公司 | System and method for continuously producing sodium thiocyanate-free and by-producing ammonium sulfate from cracking furnace gas |
| CN111362279B (en) * | 2020-04-23 | 2024-05-07 | 营口德瑞化工有限公司 | System and method for continuously producing sodium cyanide without sulfur and by-producing ammonium sulfate by cracking furnace gas |
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