CN116463148A - Method and device for producing hydrogen by injecting water vapor-coke powder into converter flue - Google Patents
Method and device for producing hydrogen by injecting water vapor-coke powder into converter flue Download PDFInfo
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- CN116463148A CN116463148A CN202310429804.2A CN202310429804A CN116463148A CN 116463148 A CN116463148 A CN 116463148A CN 202310429804 A CN202310429804 A CN 202310429804A CN 116463148 A CN116463148 A CN 116463148A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000001257 hydrogen Substances 0.000 title claims abstract description 14
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 77
- 239000007789 gas Substances 0.000 claims abstract description 76
- 238000001816 cooling Methods 0.000 claims abstract description 37
- 238000009834 vaporization Methods 0.000 claims abstract description 33
- 230000008016 vaporization Effects 0.000 claims abstract description 32
- 239000007921 spray Substances 0.000 claims abstract description 25
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 239000003546 flue gas Substances 0.000 claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 15
- 229940098458 powder spray Drugs 0.000 claims abstract description 14
- 238000003860 storage Methods 0.000 claims abstract description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 3
- 238000005507 spraying Methods 0.000 claims abstract 2
- 238000002347 injection Methods 0.000 claims description 22
- 239000007924 injection Substances 0.000 claims description 22
- 238000003723 Smelting Methods 0.000 claims description 11
- 239000012717 electrostatic precipitator Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 239000012159 carrier gas Substances 0.000 claims description 7
- 239000000428 dust Substances 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 238000007664 blowing Methods 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 3
- 238000005108 dry cleaning Methods 0.000 claims description 2
- 230000001681 protective effect Effects 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 239000002918 waste heat Substances 0.000 abstract description 2
- 238000005272 metallurgy Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000032258 transport Effects 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000009865 steel metallurgy Methods 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J1/00—Production of fuel gases by carburetting air or other gases without pyrolysis
- C10J1/26—Production of fuel gases by carburetting air or other gases without pyrolysis using raised temperatures or pressures
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/725—Redox processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/024—Dust removal by filtration
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/028—Dust removal by electrostatic precipitation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Dispersion Chemistry (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
本发明提供一种转炉烟道喷吹水蒸气‑焦粉生产氢气的方法和装置，属于冶金技术领域。包括：在转炉汽化冷却烟道的固定段烟道入口处安装焦粉喷枪和水蒸气喷枪，分别将焦粉、水蒸气喷入转炉的汽化冷却烟道，焦粉与水蒸气、烟气中的CO2和O2利用烟气中的热量分别发生化学反应并生成含H2和CO气体的混合气，混合气中的H2和CO气体经过变压吸附塔进行分离，分离得到浓度为15％～25％的H2和74％～84％的CO气体，占煤气总体积的98％～99％，分别储存在H2储存罐和煤气柜中。本发明能够充分利用转炉烟道余热资源，减轻烟道汽化冷却负担，生产H2，净化煤气，提高转炉煤气的热值，从源头实现了转炉节能减排。
The invention provides a method and a device for producing hydrogen by injecting steam-coke powder into a converter flue, belonging to the technical field of metallurgy. Including: installing a coke powder spray gun and a water vapor spray gun at the entrance of the fixed section of the converter vaporization cooling flue, spraying coke powder and water vapor into the vaporization cooling flue of the converter respectively, coke powder and water vapor, CO2 and O2 in the flue gas use the heat in the flue gas to undergo chemical reactions respectively to generate a mixed gas containing H2 and CO gas, and the H2 and CO gas in the mixed gas are separated through a pressure swing adsorption tower to obtain H2 and 7 with a concentration of 15% to 25%. 4% to 84% CO gas, accounting for 98% to 99% of the total gas volume, is stored in the H2 storage tank and the gas cabinet respectively. The invention can make full use of the waste heat resources of the converter flue, reduce the burden of vaporization and cooling of the flue, produce H2 , purify the gas, increase the calorific value of the converter gas, and realize the energy saving and emission reduction of the converter from the source.
Description
技术领域technical field
本发明属于钢铁冶金技术领域，特别涉及一种转炉烟道喷吹水蒸气-焦粉生产氢气的方法和装置。The invention belongs to the technical field of iron and steel metallurgy, and in particular relates to a method and a device for producing hydrogen by injecting steam-coke powder into a converter flue.
背景技术Background technique
目前，大多数钢铁企业使用转炉煤气进行发电，供应家庭供暖和其他燃料，但是较少工厂具有较高的转化回收水平。炼钢工艺所产生的转炉煤气主要成分是CO和CO2，约占煤气总体积的95％，其中CO占60％～80％，CO2占15％～20％。转炉煤气的热值很大程度上取决于CO的含量，一般来说，转炉煤气中CO高于55％时，转炉煤气被称为高发热值的高品质煤气。此外，CO2的产生量也是不可忽略的，每年不经过任何处理就排放至空气中的CO2超过2.6亿吨。因此，减少CO2排放并提高转炉煤气的热值对于实现可持续发展具有重要意义。Currently, most steel companies use converter gas for power generation, home heating and other fuels, but fewer plants have high conversion recovery levels. The main components of converter gas produced by the steelmaking process are CO and CO 2 , accounting for about 95% of the total gas volume, of which CO accounts for 60%-80%, and CO 2 accounts for 15%-20%. The calorific value of converter gas largely depends on the content of CO. Generally speaking, when CO in converter gas is higher than 55%, converter gas is called high-quality gas with high calorific value. In addition, the production of CO 2 is not negligible, and the amount of CO 2 emitted into the air without any treatment exceeds 260 million tons every year. Therefore, reducing CO2 emissions and increasing the calorific value of converter gas are of great significance for achieving sustainable development.
转炉冶炼过程烟气进入炉口上方的微负压烟罩时温度约为1500℃，主要成分为CO、CO2、O2。一般情况下将其通过汽化冷却烟道冷却至800～1000℃，再对其进行喷水或喷水蒸汽，使烟气急速降温至200℃以下，这种技术对于转炉烟气携带的热量并未有效的利用，浪费了能源。The temperature of the flue gas in the converter smelting process is about 1500°C when it enters the micro-negative pressure fume hood above the furnace mouth, and the main components are CO, CO 2 and O 2 . Generally, it is cooled to 800-1000°C through the vaporization cooling flue, and then sprayed with water or water steam to rapidly cool the flue gas below 200°C. This technology does not effectively use the heat carried by the converter flue gas and wastes energy.
焦粉和水蒸气、烟气中的CO2、O2的反应属于气-固接触反应，方程式如(1)、(3)、(5)所示：The reaction between coke powder and water vapor, CO 2 and O 2 in the flue gas belongs to the gas-solid contact reaction, and the equations are shown in (1), (3) and (5):
C(s)+H2O(g)＝CO(g)+H2(g) (1)C (s) + H 2 O (g) = CO (g) + H 2(g) (1)
ΔrGθ＝-141T+133260(J/mol) (2)Δ r G θ = -141T+133260(J/mol) (2)
C(s)+CO2(g)＝2CO(g) (3)C (s) + CO 2(g) = 2CO (g) (3)
ΔrGθ＝-167.86T+162760(J/mol) (4)Δ r G θ ＝-167.86T+162760(J/mol) (4)
2C(s)+O2(g)＝2CO(g) (5)2C (s) + O 2(g) = 2CO (g) (5)
ΔrGθ＝-167.78T+232630(J/mol) (6)Δ r G θ ＝-167.78T+232630(J/mol) (6)
反应(1)和(3)为吸热反应，(5)为放热反应，由式(2)、(4)、(6)计算可知，标准状态下，反应(1)、(3)、(5)发生的最低温度分别为：945K、970K、1386K。转炉烟道内烟气温度为1500℃左右，故可满足以上反应的进行。综上，在转炉烟道内喷吹水蒸气-焦粉生产氢气的方法是可行的，在生产氢气加以利用的同时提高转炉煤气的热值。Reactions (1) and (3) are endothermic reactions, and (5) is an exothermic reaction. It can be seen from formulas (2), (4) and (6) that under standard conditions, the lowest temperatures at which reactions (1), (3), and (5) occur are: 945K, 970K, and 1386K, respectively. The flue gas temperature in the converter flue is about 1500°C, so it can satisfy the above reaction. To sum up, it is feasible to produce hydrogen by injecting water vapor-coke powder in the converter flue, and increase the calorific value of converter gas while producing hydrogen and utilizing it.
发明内容Contents of the invention
现有技术中转炉煤气热值低，回收量小且CO2排放量大，烟道余热资源浪费严重，亟需提供一种新的方法对其加以利用并生产有益产品。In the prior art, converter gas has a low calorific value, a small amount of recovery and a large amount of CO 2 emissions, and a serious waste of flue waste heat resources. It is urgent to provide a new method to utilize it and produce beneficial products.
为解决上述技术问题，本发明提供如下技术方案：In order to solve the above technical problems, the present invention provides the following technical solutions:
一种转炉烟道喷吹水蒸气-焦粉生产氢气的方法，包括：A method for producing hydrogen by injecting steam into a converter flue-coke powder, comprising:
在转炉汽化冷却烟道的固定段烟道入口处安装焦粉喷枪和水蒸气喷枪，分别将焦粉、水蒸气喷入转炉的汽化冷却烟道，焦粉与水蒸气、烟气中的CO2和O2利用烟气中的热量分别发生反应并生成含H2和CO气体的混合气，混合气中的H2和CO气体经过变压吸附塔进行分离，分别储存在H2储存罐和煤气柜中。A coke powder spray gun and a water vapor spray gun are installed at the entrance of the fixed section of the converter vaporization cooling flue, and the coke powder and water vapor are sprayed into the vaporization cooling flue of the converter respectively. The coke powder, water vapor, and CO2 and O2 in the flue gas use the heat in the flue gas to react respectively to generate a mixed gas containing H2 and CO gas.
可选地，水蒸气在转炉冶炼过程自循环利用，全部引自储存在蓄热器内的饱和蒸汽，经过水蒸气喷枪喷入转炉的汽化冷却烟道。具体的，汽化冷却烟道的末端将汽化冷却烟道产生的汽水混合物输送至汽包，汽包将汽水混合物分离，分离得到的饱和蒸汽经管道送至蓄热器，而分离出来的液态水重新输送至汽化冷却烟道的前端。本发明主要是为了应用转炉汽化冷却烟道产生的水蒸气，过程使用的水蒸气全部来自于本炉体冶炼时汽化冷却烟道产生的饱和蒸汽，形成自循环系统，而无需外界提供。Optionally, the water vapor is self-recycled in the converter smelting process, all of which are drawn from the saturated steam stored in the heat accumulator, and sprayed into the vaporization cooling flue of the converter through a steam spray gun. Specifically, the end of the evaporative cooling flue transports the steam-water mixture generated by the evaporative cooling flue to the steam drum, and the steam drum separates the steam-water mixture, and the separated saturated steam is sent to the heat accumulator through the pipeline, and the separated liquid water is re-delivered to the front end of the evaporative cooling flue. The present invention is mainly to use the water vapor produced by the vaporization cooling flue of the converter. The water vapor used in the process all comes from the saturated steam generated by the vaporization cooling flue during the smelting of the furnace body, forming a self-circulation system without external supply.
可选地，焦粉粒径为200～300目，采用双层环缝式喷枪喷吹，内管以CO2气体为载气输送焦粉，环缝采用CO2气体作为保护气，内管载气CO2的流量为1200～2000Nm3/h，环缝载气CO2流量为100～300Nm3/h，CO2气源压力不低于1.5MPa。Optionally, the particle size of the coke powder is 200-300 mesh , and it is sprayed by double-layer annular slit spray guns. The inner pipe uses CO 2 gas as the carrier gas to transport the coke powder, and the annular slit uses CO 2 gas as the protective gas .
可选地，水蒸气和焦粉在转炉吹氧冶炼开始后的4～15min内进行喷吹，喷吹水蒸气流量5000～10000Nm3/h，喷吹焦粉流量100～300kg/min，水蒸气和焦粉的喷吹质量比为0.9～1.5。Optionally, water vapor and coke powder are injected within 4 to 15 minutes after the start of the converter oxygen blowing smelting, the injection steam flow rate is 5000-10000Nm 3 /h, the injection coke powder flow rate is 100-300kg/min, and the injection mass ratio of water vapor and coke powder is 0.9-1.5.
可选地，汽化冷却烟道内产生的混合气体经过蒸发冷却器、焦粉过滤筛网、电除尘器后，经风机输送至变压吸附塔依次去除富余的水蒸气、焦粉、粉尘、CO2等，并对CO和H2进行分离，得到高纯度的CO和H2气体。Optionally, the mixed gas generated in the evaporative cooling flue passes through the evaporative cooler, coke powder filter screen, and electrostatic precipitator, and then is transported to the pressure swing adsorption tower through the fan to remove excess water vapor, coke powder, dust, CO2 , etc., and separate CO and H2 to obtain high-purity CO and H2 gas.
可选地，本方法适用于安装有干法净化与回收除尘系统的吹氧转炉。Optionally, this method is applicable to a converter equipped with dry cleaning and recovery dedusting system.
一种转炉烟道喷吹水蒸气-焦粉生产氢气的装置，包括：A device for producing hydrogen by injecting water vapor into the flue of a converter-coke powder, comprising:
转炉、汽化冷却烟道、蓄热器、CO2气源、焦粉喷射罐、焦粉喷枪、水蒸气喷枪、蒸发冷却器、焦粉过滤筛网、电除尘器、风机、第一变压吸附塔、第二变压吸附塔、H2储存罐、煤气冷却器、煤气柜；Converter, vaporization cooling flue, heat accumulator, CO2 gas source, coke powder injection tank, coke powder spray gun, water vapor spray gun, evaporative cooler, coke powder filter screen, electrostatic precipitator, fan, first PSA tower, second PSA tower, H2 storage tank, gas cooler, gas cabinet;
汽化冷却烟道设置于转炉炉口上方；The vaporization cooling flue is set above the furnace mouth of the converter;
水蒸气喷枪连接蓄热器和汽化冷却烟道；The steam spray gun is connected to the heat accumulator and the vaporization cooling flue;
焦粉喷枪连接于汽化冷却烟道，并与CO2气源和焦粉喷射罐连通；The coke powder spray gun is connected to the vaporization cooling flue, and communicated with the CO2 gas source and the coke powder spray tank;
汽化冷却烟道出口依次与蒸发冷却器、焦粉过滤筛网、电除尘器、风机、第一变压吸附塔、第二变压吸附塔连接；The outlet of the vaporization cooling flue is sequentially connected with the evaporative cooler, the coke powder filter screen, the electrostatic precipitator, the fan, the first pressure swing adsorption tower, and the second pressure swing adsorption tower;
第二变压吸附塔出口分别连接H2储存罐与煤气冷却器，煤气冷却器还与煤气柜连接。The outlet of the second pressure swing adsorption tower is respectively connected to the H2 storage tank and the gas cooler, and the gas cooler is also connected to the gas cabinet.
可选地，焦粉过滤筛网可将焦粉存留而使烟道内气体和烟尘通过，喷入烟道的未参与反应的焦粉通过焦粉过滤筛网过滤并重新输送至焦粉喷射罐进行循环利用。由于汽化冷却烟道内烟气流动速度非常快，焦粉和水蒸气喷入后可能反应不完全，反应率还有待提升，若不将焦粉重新过滤，不仅造成了焦粉的浪费，还加重了烟道除尘的负担。本装置在蒸发冷却器后增添焦粉过滤筛网，利用焦粉和烟尘粒径不同对焦粉进行过滤，实现了焦粉的循环利用。Optionally, the coke powder filter screen can retain the coke powder to allow the gas and smoke in the flue to pass through, and the coke powder injected into the flue that does not participate in the reaction is filtered through the coke powder filter screen and re-transported to the coke powder injection tank for recycling. Due to the very fast flow of flue gas in the vaporization cooling flue, coke powder and water vapor may react incompletely after injection, and the reaction rate needs to be improved. If the coke powder is not re-filtered, it will not only cause waste of coke powder, but also increase the burden of dust removal in the flue. In this device, a coke powder filter screen is added after the evaporative cooler, and the coke powder with different particle sizes of the coke powder and smoke dust is used to filter the coke powder, thereby realizing the recycling of the coke powder.
可选地，水蒸气喷枪数量根据转炉公称容量选择1～6支，焦粉喷枪数量根据转炉公称容量选择1～6支，多支喷枪通过分配器进行连接。Optionally, the number of steam spray guns is selected from 1 to 6 according to the nominal capacity of the converter, the number of coke powder spray guns is selected from 1 to 6 according to the nominal capacity of the converter, and multiple spray guns are connected through a distributor.
本发明提供的技术方案带来的有益效果至少包括：The beneficial effects brought by the technical solution provided by the present invention at least include:
本发明在转炉烟道内喷吹水蒸气和焦粉，水蒸气与焦粉利用烟气中的热量发生反应生成H2，喷入的水蒸气全部来自于转炉汽化冷却过程产生的饱和蒸汽，实现了水蒸气在转炉冶炼流程的自循环利用，回收后的氢气可应用于钢铁生产流程的其他工序；烟道内过量的焦粉与烟气中携带的O2和CO2亦可发生反应，生成CO，净化煤气纯度，提高煤气的热值；此外，焦粉与水蒸气、CO2的反应均为吸热反应，反应在吹炼过程消耗烟道内富余的高温余热且无需提供额外的热量，烟气实时温度降低700～800℃，减轻了汽化冷却和除尘的压力，从源头对转炉烟气余热进行利用；本发明应用过程水蒸气反应率达85％以上，CO2反应率达90％以上，应用后得到体积浓度为15％～25％的H2和74％～84％的CO气体，占煤气总体积的98％～99％。经变压吸附塔分离后单炉次回收氢气2000～8000Nm3，回收CO提高3000～16000Nm3。本发明在转炉烟道内喷吹水蒸气和焦粉，水蒸气与焦粉利用烟气中的热量发生反应生成H 2 ，喷入的水蒸气全部来自于转炉汽化冷却过程产生的饱和蒸汽，实现了水蒸气在转炉冶炼流程的自循环利用，回收后的氢气可应用于钢铁生产流程的其他工序；烟道内过量的焦粉与烟气中携带的O 2和CO 2亦可发生反应，生成CO，净化煤气纯度，提高煤气的热值；此外，焦粉与水蒸气、CO 2的反应均为吸热反应，反应在吹炼过程消耗烟道内富余的高温余热且无需提供额外的热量，烟气实时温度降低700～800℃，减轻了汽化冷却和除尘的压力，从源头对转炉烟气余热进行利用；本发明应用过程水蒸气反应率达85％以上，CO 2反应率达90％以上，应用后得到体积浓度为15％～25％的H 2和74％～84％的CO气体，占煤气总体积的98％～99％。 After being separated by the pressure swing adsorption tower, the hydrogen recovery in a single furnace is 2000-8000Nm 3 , and the recovery of CO is increased by 3000-16000Nm 3 .
附图说明Description of drawings
为了更清楚地说明本发明实施例中的技术方案，下面将对实施例描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他的附图。In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the following will briefly introduce the accompanying drawings that need to be used in the description of the embodiments. Obviously, the accompanying drawings in the following description are only some embodiments of the present invention. For those of ordinary skill in the art, other drawings can also be obtained based on these drawings without creative work.
图1为本发明转炉烟道喷吹水蒸气-焦粉生产氢气的装置结构示意图；Fig. 1 is the schematic diagram of the device structure of converter flue injection water vapor-coke powder production hydrogen of the present invention;
其中：1-转炉本体，2-水蒸气喷枪，3-蓄热器，4-汽包，5-焦粉喷枪，6-焦粉喷射罐，7-CO2气源，8-汽化冷却烟道，9-蒸发冷却器，10-焦粉过滤筛网，11-电除尘器，12-风机，13—1-变压吸附塔1，13-2-变压吸附塔2，14-H2储存罐，15-煤气冷却器，16-煤气柜，17-加压站。Among them: 1-converter body, 2-water vapor spray gun, 3-regenerator, 4-steam drum, 5-coke powder spray gun, 6-coke powder spray tank, 7- CO2 gas source, 8-vaporization cooling flue, 9-evaporative cooler, 10-coke powder filter screen, 11-electric dust collector, 12-fan, 13—1-pressure swing adsorption tower 1, 13-2-pressure swing adsorption tower 2, 14-H 2 storage tank, 15-gas cooler , 16-gas tank, 17-pressurization station.
具体实施方式Detailed ways
为使本发明的目的、技术方案和优点更加清楚，下面将结合附图及具体实施例对本发明的技术方案进行详细的描述。In order to make the object, technical solution and advantages of the present invention clearer, the technical solution of the present invention will be described in detail below with reference to the drawings and specific embodiments.
实施例1Example 1
本实施例为用于120t转炉的烟道喷吹水蒸气-焦粉生产氢气的方法。This embodiment is a method for producing hydrogen by injecting water vapor-coke powder into the flue of a 120t converter.
120t转炉的烟道喷吹水蒸气-焦粉生产氢气的方法在转炉吹氧冶炼过程将焦粉和水蒸气连续喷入汽化冷却烟道，焦粉与喷入的水蒸气和CO2、烟气中的CO2和O2气体反应得到纯净的H2和CO气体。120t converter flue injection steam-coke powder hydrogen production method During the oxygen blowing smelting process of the converter, coke powder and water vapor are continuously sprayed into the vaporization cooling flue, coke powder reacts with the injected water vapor and CO 2 , and CO 2 and O 2 gases in the flue gas to obtain pure H 2 and CO gas.
所述水蒸气采用蓄热器3内的饱和蒸汽，喷枪2将水蒸气从蓄热器3喷入汽化冷却烟道8；The water vapor adopts the saturated steam in the heat accumulator 3, and the spray gun 2 sprays the water vapor from the heat accumulator 3 into the vaporization cooling flue 8;
所述焦粉以CO2气源7为载气从焦粉喷射罐6通过喷枪5喷入汽化冷却烟道8；The coke powder is sprayed into the vaporization cooling flue 8 from the coke powder injection tank 6 through the spray gun 5 with the CO gas source 7 as the carrier gas;
所述水蒸气和焦粉在转炉吹氧冶炼开始后的5～13min内进行喷吹，水蒸气和焦粉的质量比为0.96，使用2支水蒸气喷枪，喷吹速度为9000Nm3/h，使用1支焦粉喷枪，焦粉粒径为200～300目，焦粉喷吹速度为250kg/min，中心管载气CO2喷吹速度为1500Nm3/h，环缝气CO2喷吹速度为150Nm3/h；The water vapor and coke powder are injected within 5-13 minutes after the start of oxygen blowing smelting in the converter, the mass ratio of water vapor and coke powder is 0.96, two water vapor spray guns are used, the injection speed is 9000Nm 3 /h, and one coke powder spray gun is used, the coke powder particle size is 200-300 mesh, the coke powder injection speed is 250kg/min, and the central tube carrier gas CO 2 injection speed is 1500Nm 3 /h. The injection speed of slit gas CO 2 is 150Nm 3 /h;
所述烟道内产生的气体经过蒸发冷却器9、焦粉过滤筛网10和电除尘器11后，经风机12输送至变压吸附塔13-1和13-2后依次去除富余的水蒸气、焦粉、粉尘、CO2等，并对CO和H2进行分离，得到高纯度的CO和H2气体。The gas generated in the flue passes through the evaporative cooler 9, the coke powder filter screen 10 and the electrostatic precipitator 11, and then is transported to the pressure swing adsorption towers 13-1 and 13-2 by the fan 12, and then the excess water vapor, coke powder, dust, CO2 , etc. are sequentially removed, and CO and H2 are separated to obtain high-purity CO and H2 gas.
采用本实施例的方法前，120t转炉单炉次平均产生烟气9500Nm3，其中CO比例为80％，CO2比例为15％，O2比例为1.8％。结果表明，采用本实施例的方法后，单炉次平均消耗水蒸气2600Nm3，消耗CO2气体250Nm3，消耗焦粉1950kg，烟道内H2和CO的体积占比分别为15％和83％，分离后得到2200Nm3的H2和12200Nm3的CO气体。该方法水蒸气平均反应率为84.6％，CO2平均反应率为92％，CO气体生成量增加4600Nm3，烟道内实时温度平均下降750℃，减轻了烟道汽化冷却的负担，生产清洁气体H2以供应用的同时净化转炉煤气的纯度。Before adopting the method of this embodiment, a single furnace of 120 t converter produces an average flue gas of 9500Nm 3 , wherein the proportion of CO is 80%, the proportion of CO 2 is 15%, and the proportion of O 2 is 1.8%. The results show that after adopting the method of this example, the average water vapor consumption per furnace is 2600Nm 3 , CO 2 gas is 250Nm 3 , and coke powder is 1950kg. The volume ratios of H2 and CO in the flue are 15% and 83% respectively. After separation, 2200Nm3 of H2 and 12200Nm3 of CO gas are obtained. In this method, the average reaction rate of water vapor is 84.6%, the average reaction rate of CO2 is 92%, the amount of CO gas generated increases by 4600Nm3 , and the real-time temperature in the flue decreases by an average of 750°C, which reduces the burden of vaporization and cooling of the flue, and produces clean gas H2 for use while purifying the purity of converter gas.
实施例2Example 2
本实施例为用于300t转炉的烟道喷吹水蒸气-焦粉生产氢气的方法。This embodiment is a method for producing hydrogen by injecting water vapor-coke powder into the flue of a 300t converter.
300t转炉的烟道喷吹水蒸气-焦粉生产氢气的方法在转炉吹氧冶炼过程将焦粉和水蒸气连续喷入汽化冷却烟道，焦粉与喷入的水蒸气和CO2、烟气中的CO2和O2气体反应得到纯净的H2和CO气体。300t converter flue injection steam-coke powder hydrogen production method During the oxygen blowing smelting process of the converter, coke powder and water vapor are continuously sprayed into the vaporization cooling flue, coke powder reacts with injected water vapor and CO 2 , and CO 2 and O 2 gases in the flue gas to obtain pure H 2 and CO gas.
所述水蒸气采用蓄热器3内的饱和蒸汽，喷枪2将水蒸气从蓄热器3喷入汽化冷却烟道8；The water vapor adopts the saturated steam in the heat accumulator 3, and the spray gun 2 sprays the water vapor from the heat accumulator 3 into the vaporization cooling flue 8;
所述焦粉以CO2气源7为载气从焦粉喷射罐6通过喷枪5喷入汽化冷却烟道8；The coke powder is sprayed into the vaporization cooling flue 8 from the coke powder injection tank 6 through the spray gun 5 with the CO gas source 7 as the carrier gas;
所述水蒸气和焦粉在转炉吹氧冶炼开始后的5～14min内进行喷吹，水蒸气和焦粉的质量比为0.97，使用6支水蒸气喷枪，喷吹速度为8000Nm3/h，使用3支焦粉喷枪，焦粉粒径为200～300目，焦粉喷吹速度为220kg/min，中心管载气CO2速度为1500Nm3/h，环缝气CO2速度为150Nm3/h；The water vapor and coke powder are injected within 5 to 14 minutes after the start of the converter oxygen blowing smelting. The mass ratio of water vapor and coke powder is 0.97. Six water vapor spray guns are used with an injection speed of 8000Nm 3 /h. The CO 2 rate is 150Nm 3 / h;
所述烟道内产生的气体经过蒸发冷却器9、焦粉过滤筛网10和电除尘器11后，经风机12输送至变压吸附塔13-1和13-2后依次去除富余的水蒸气、焦粉、粉尘、CO2等，并对CO和H2进行分离，得到高纯度的CO和H2气体。The gas generated in the flue passes through the evaporative cooler 9, the coke powder filter screen 10 and the electrostatic precipitator 11, and then is transported to the pressure swing adsorption towers 13-1 and 13-2 by the fan 12, and then the excess water vapor, coke powder, dust, CO2 , etc. are sequentially removed, and CO and H2 are separated to obtain high-purity CO and H2 gas.
采用本实施例的方法前，300t转炉单炉次平均产生烟气22500Nm3，其中CO比例为75％，CO2比例为20％，O2比例为1.5％。结果表明，采用本实施例的方法后，单炉次平均消耗水蒸气7900Nm3，消耗CO2气体850Nm3，消耗焦粉6200kg，烟道内H2和CO的体积占比分别为17.57％和80.5％，分离后得到7200Nm3的H2和33000Nm3的CO气体。该方法水蒸气平均反应率为86％，CO2平均反应率为91％，CO气体生成量增加16125Nm3，烟道内实时温度平均下降770℃，减轻了烟道汽化冷却的负担，生产清洁气体H2以供应用的同时净化转炉煤气的纯度。Before adopting the method of this embodiment, a single furnace of 300 t converter produces an average flue gas of 22500Nm 3 , of which the proportion of CO is 75%, the proportion of CO 2 is 20%, and the proportion of O 2 is 1.5%. The results show that after adopting the method of this example, the average consumption of water vapor is 7900Nm 3 , CO 2 gas is 850Nm 3 , coke powder is 6200kg, and the volume ratios of H2 and CO in the flue are 17.57% and 80.5%, respectively. After separation, 7200Nm3 of H2 and 33000Nm3 of CO gas are obtained. In this method, the average reaction rate of water vapor is 86%, the average reaction rate of CO2 is 91%, the amount of CO gas generated increases by 16125Nm3 , and the real-time temperature in the flue decreases by an average of 770°C, which reduces the burden of vaporization and cooling of the flue, and produces clean gas H2 for use while purifying the purity of converter gas.
综上，本发明的冶炼方法和装置结构简单，利于工业大规模生产和推广。To sum up, the smelting method and device of the present invention have a simple structure, which is beneficial to large-scale industrial production and popularization.
以上所述，仅为本发明的具体实施方式，但本发明的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本发明揭露的技术范围内，可轻易想到变化或替换，都应涵盖在本发明的保护范围之内。因此，本发明的保护范围应以所述权利要求的保护范围为准。The above is only a specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art can easily think of changes or substitutions within the technical scope disclosed in the present invention, and all should be covered within the protection scope of the present invention. Therefore, the protection scope of the present invention should be determined by the protection scope of the claims.
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