CN104930865A - Energy-saving blast furnace system utilizing waste heat and excessive pressure to supply oxygen-enriched air itself - Google Patents
Energy-saving blast furnace system utilizing waste heat and excessive pressure to supply oxygen-enriched air itself Download PDFInfo
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 76
- 239000001301 oxygen Substances 0.000 title claims abstract description 76
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 76
- 239000002918 waste heat Substances 0.000 title claims abstract description 29
- 238000003795 desorption Methods 0.000 claims abstract description 173
- 238000010521 absorption reaction Methods 0.000 claims abstract description 116
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 100
- 239000003546 flue gas Substances 0.000 claims abstract description 100
- 238000004519 manufacturing process Methods 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims description 51
- 238000011084 recovery Methods 0.000 claims description 19
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 6
- 229910052742 iron Inorganic materials 0.000 claims description 3
- 229910000805 Pig iron Inorganic materials 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract description 4
- 239000000571 coke Substances 0.000 abstract description 3
- 238000001179 sorption measurement Methods 0.000 description 57
- 239000007789 gas Substances 0.000 description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 238000002336 sorption--desorption measurement Methods 0.000 description 13
- 239000000428 dust Substances 0.000 description 8
- 239000002808 molecular sieve Substances 0.000 description 8
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 229910000831 Steel Inorganic materials 0.000 description 5
- 239000003245 coal Substances 0.000 description 5
- 238000002347 injection Methods 0.000 description 5
- 239000007924 injection Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 239000010959 steel Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229910001341 Crude steel Inorganic materials 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 238000003303 reheating Methods 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000011900 installation process Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
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Abstract
本发明公开了一种利用余热余压自供富氧空气的节能高炉系统，包括炼铁子系统以及富氧制取子系统，富氧制取子系统包括两组吸/脱附塔以及对吸/脱附塔提供压缩空气的压缩机，每个吸/脱附塔内设有烟气通道、空气通道和换热介质通道，其中烟气通道的进、出口分别通过管路与炼铁子系统的烟气出口和烟囱相连，空气通道的进、出口分别通过管路与压缩机出口、炼铁子系统的富氧空气入口相连；两组吸/脱附塔中的换热介质通道首尾连通形成实现吸附热量回用的循环通道；所述烟气通道、空气通道上设有阀门。本发明不但提高了余热的回收利用率，而且减少了高炉的焦炭消耗和提高了生铁产量。
The invention discloses an energy-saving blast furnace system that uses waste heat and pressure to self-supply oxygen-enriched air, including an ironmaking subsystem and an oxygen-enriched production subsystem. The desorption tower provides a compressor for compressing air. Each absorption/desorption tower is equipped with a flue gas channel, an air channel and a heat exchange medium channel. The flue gas outlet is connected to the chimney, and the inlet and outlet of the air channel are respectively connected to the compressor outlet and the oxygen-enriched air inlet of the ironmaking subsystem through pipelines; the end-to-end connection of the heat exchange medium channels in the two groups of absorption/desorption towers is realized A circulation channel for recycling the absorbed heat; the flue gas channel and the air channel are provided with valves. The invention not only improves the recycling rate of waste heat, but also reduces the coke consumption of the blast furnace and increases the pig iron output.
Description
技术领域technical field
本发明属于高炉设计技术领域，具体是涉及一种利用余热余压自供富氧空气的节能高炉系统。The invention belongs to the technical field of blast furnace design, and in particular relates to an energy-saving blast furnace system which uses waste heat and pressure to self-supply oxygen-enriched air.
背景技术Background technique
钢铁产业是国民经济的命脉，根据全球钢铁产量和不锈钢产量报告，2014年中国以8.23亿吨的粗钢产量位居世界第一，占全球粗钢产量的49.5％。我国钢铁工业余热资源量高达455.1kg标准煤/吨钢，目前回收利用率仅为日本、德国等发达国家的一半。可见我国钢铁工业余热资源回收潜力巨大。The steel industry is the lifeblood of the national economy. According to the global steel production and stainless steel production reports, China ranked first in the world with 823 million tons of crude steel production in 2014, accounting for 49.5% of the global crude steel production. The amount of waste heat resources in my country's iron and steel industry is as high as 455.1kg standard coal/ton of steel, and the current recycling rate is only half of that of developed countries such as Japan and Germany. It can be seen that the recovery potential of waste heat resources in my country's iron and steel industry is huge.
与此同时，高炉富氧喷煤技术的应用大幅降低了焦炭耗量和生铁成本，提高了生铁生产效率。但要提高喷煤比，实现大喷吹量，提高富氧率是必不可少的手段。由于各企业高炉富氧的氧气来源大多是炼钢生产富余氧气，造成富氧率不稳定，氧气供应没有保证，不利于炉况的稳定，也不利于充分发挥富氧喷煤技术的作用。At the same time, the application of blast furnace oxygen-enriched coal injection technology has greatly reduced coke consumption and pig iron cost, and improved pig iron production efficiency. However, to increase the coal injection ratio and achieve a large injection volume, increasing the oxygen enrichment rate is an indispensable means. Since the source of oxygen-enriched oxygen for blast furnaces in various enterprises is mostly surplus oxygen produced by steelmaking, the oxygen-enriched rate is unstable and oxygen supply is not guaranteed, which is not conducive to the stability of furnace conditions and the full play of the role of oxygen-enriched coal injection technology.
目前，变压吸附制取富氧的技术较为成熟。变压吸附制氧富氧率很高，可以达到60％～95％，但电耗大，成本高。富氧喷煤技术使用的富氧仅需提高几个百分点就可以满足实际生产需要。如果采用变压吸附，不但消耗宝贵的电能，而且，经济性不好，很难推广应用。At present, the technology of producing oxygen enriched by pressure swing adsorption is relatively mature. The oxygen enrichment rate of pressure swing adsorption oxygen production is very high, which can reach 60% to 95%, but the power consumption is large and the cost is high. The oxygen enrichment used in the oxygen-enriched coal injection technology only needs to be increased by a few percentage points to meet the actual production needs. If pressure swing adsorption is adopted, it will not only consume precious electric energy, but also have poor economic efficiency, making it difficult to popularize and apply it.
图1所示为传统的炼铁子系统，传统炼铁子系统主要包括：用于加热将要进入高炉反应的空气的热风炉，与所述热风炉的出气口连通的高炉，与所述高炉的出气口连通的除尘装置，与所述除尘装置的出口连通的透平机以及回热器，透平机出口通过管路与热风炉的高温煤气入口连通，热风炉的热风炉烟气出口与所述回热器的高温烟气入口连通，回热器的高温烟气出口连接烟囱。所述热风炉排放的高温热风炉烟气用于加热进入热风炉的空气，以利用系统废热能量；所述透平机利用高炉煤气的余压能量输出机械功，所述透平机出口的低压高炉煤气送至热风炉燃烧用于预热富氧空气。由图1可知，目前热风炉高温烟气余热利用仍然以预热助燃空气、预热高炉煤气为主，只利用了其中一小部分的能量，还有一大部分的能量都是以热量的形式排放掉了，没有得到充分利用。Figure 1 shows the traditional ironmaking subsystem, the traditional ironmaking subsystem mainly includes: a hot blast stove for heating the air that will enter the blast furnace for reaction, a blast furnace communicated with the gas outlet of the hot blast stove, and the blast furnace The dust removal device connected to the gas outlet, the turbine and the regenerator connected to the outlet of the dust removal device, the turbine outlet is connected to the high-temperature gas inlet of the hot blast stove through a pipeline, and the hot blast stove flue gas outlet of the hot blast stove is connected to the The high-temperature flue gas inlet of the regenerator is connected, and the high-temperature flue gas outlet of the regenerator is connected to the chimney. The high-temperature hot blast stove flue gas discharged from the hot blast stove is used to heat the air entering the hot blast stove to utilize the waste heat energy of the system; the turbine uses the residual pressure energy of the blast furnace gas to output mechanical work, and the low pressure at the outlet of the turbine The blast furnace gas is sent to the hot stove for combustion to preheat the oxygen-enriched air. It can be seen from Figure 1 that at present, the waste heat utilization of high-temperature flue gas in hot blast stoves is still mainly preheating combustion-supporting air and blast furnace gas, only a small part of the energy is used, and most of the energy is discharged in the form of heat Dropped and underused.
发明内容Contents of the invention
本发明提供了一种利用余热余压自供富氧空气的节能高炉系统，充分利用被排放掉的热风炉烟气中的余热能量，更直接高效的利用高炉煤气余压能量，减少系统燃料消耗，降低生产成本，同时增加生铁产量。The present invention provides an energy-saving blast furnace system that uses waste heat and pressure to self-supply oxygen-enriched air, fully utilizes the waste heat energy in the exhausted hot blast stove flue gas, utilizes the blast furnace gas residual pressure energy more directly and efficiently, and reduces system fuel consumption. Reduce production costs while increasing pig iron production.
一种利用余热余压自供富氧空气的节能高炉系统，包括炼铁子系统以及富氧制取子系统，所述富氧制取子系统包括两组吸/脱附塔以及对吸/脱附塔提供压缩空气的压缩机，每个吸/脱附塔内设有烟气通道、空气通道和换热介质通道，其中烟气通道的进、出口分别通过管路与炼铁子系统的热风炉烟气出口和烟囱相连，空气通道的进、出口分别通过管路与压缩机出口、炼铁子系统的富氧空气入口相连；所述两组吸/脱附塔中的换热介质通道首尾连通形成实现吸附热量回用的循环通道；所述烟气通道、空气通道上设有阀门。An energy-saving blast furnace system that uses waste heat and pressure to self-supply oxygen-enriched air, including an ironmaking subsystem and an oxygen-enriched production subsystem. The oxygen-enriched production subsystem includes two sets of absorption/desorption towers and counter absorption/desorption The tower provides a compressor for compressing air. Each absorption/desorption tower is equipped with a flue gas channel, an air channel and a heat exchange medium channel. The inlet and outlet of the flue gas channel are respectively connected to the hot blast stove of the ironmaking subsystem The flue gas outlet is connected to the chimney, and the inlet and outlet of the air channel are respectively connected to the compressor outlet and the oxygen-enriched air inlet of the ironmaking subsystem through pipelines; the heat exchange medium channels in the two groups of absorption/desorption towers are connected end to end A circulation channel is formed to realize the recovery of adsorption heat; the flue gas channel and the air channel are provided with valves.
本发明中，利用吸附塔吸附过程中放热、脱附过程中吸热的特性，通过设置两组吸/脱附塔，同时保证两组吸/脱附塔交替的进行吸附和脱附，可实现将进行吸附过程的塔内热量回用至脱附过程中。而且利用炼铁子系统的热风炉烟气对脱附过程进行供热，进一步回收炼铁子系统的热量。通过换热介质一方面可以完成对吸附放热的回收，另一方面也可以完成对吸附过程的冷却。In the present invention, by using the characteristics of exothermic heat in the adsorption process and heat absorption in the desorption process of the adsorption tower, by setting two groups of adsorption/desorption towers, and ensuring that the two groups of adsorption/desorption towers alternately perform adsorption and desorption, it can Realize the recycling of the heat in the tower in the adsorption process to the desorption process. Moreover, the hot blast stove flue gas of the ironmaking subsystem is used to provide heat for the desorption process, and the heat of the ironmaking subsystem is further recovered. Through the heat exchange medium, on the one hand, the recovery of the heat released by adsorption can be completed, and on the other hand, the cooling of the adsorption process can also be completed.
本发明中，所述压缩机入口与大气连通，用于提供压缩空气，提高吸附效率；所述压缩机出口与吸/脱附塔空气入口连通；所述吸/脱附塔空气出口与第二换热器空气进口连通；所述第二换热器空气出口与炼铁子系统中的热风的炉富氧空气入口连通。所述热风炉的热风炉烟气出口与吸/脱附塔高温烟气入口连通，所述吸/脱附塔的高温烟气出口与第二换热器的的高温烟气入口或者烟囱连通；第二换热器的高温烟气出口与炼铁厂烟囱连通。所述吸/脱附塔的作用是用于吸附空气中的氮气，提高含氧率；系统有两个吸/脱附塔，一塔工作时一塔再生，切换使用。In the present invention, the inlet of the compressor is communicated with the atmosphere for providing compressed air to improve the adsorption efficiency; the outlet of the compressor is communicated with the air inlet of the absorption/desorption tower; the air outlet of the absorption/desorption tower is connected with the second The air inlet of the heat exchanger is connected; the air outlet of the second heat exchanger is connected with the furnace oxygen-enriched air inlet of the hot blast in the ironmaking subsystem. The hot blast stove flue gas outlet of the hot blast stove communicates with the high-temperature flue gas inlet of the absorption/desorption tower, and the high-temperature flue gas outlet of the absorption/desorption tower communicates with the high-temperature flue gas inlet or chimney of the second heat exchanger; The high-temperature flue gas outlet of the second heat exchanger communicates with the ironworks chimney. The function of the absorption/desorption tower is to absorb nitrogen in the air and increase the oxygen content; the system has two absorption/desorption towers, one tower is regenerated when one tower is working, and the other tower is used for switching.
作为优选，所述空气通道的出口和入口部位的管路上均设有阀门。由于吸附过程在高压下进行，所以在一组吸/脱附塔进行吸附的过程中，需要将另外一个脱附过程中的吸/脱附塔的空气通道的两端关闭，避免富氧空气进入到脱附状态下吸/脱附塔的空气通道内。Preferably, valves are provided on the pipelines at the outlet and the inlet of the air channel. Since the adsorption process is carried out under high pressure, during the adsorption process of one group of adsorption/desorption towers, it is necessary to close both ends of the air channel of the other adsorption/desorption tower in the desorption process to avoid the entry of oxygen-enriched air Into the air channel of the adsorption/desorption tower in the desorption state.
作为优选，两组换热介质通道一侧的两个第一端之间通过动力阀门组导通，所述动力阀门组包括：As a preference, the two first ends on one side of the two sets of heat exchange medium passages are connected through a dynamic valve set, and the dynamic valve set includes:
换热介质泵，所述换热介质泵用于对换热介质提供动力；A heat exchange medium pump, the heat exchange medium pump is used to provide power to the heat exchange medium;
分别设置在换热介质泵出口与两个第一端之间管路上的第一阀门、第二阀门；A first valve and a second valve respectively arranged on the pipeline between the outlet of the heat exchange medium pump and the two first ends;
分别设置在换热介质泵入口与两个第一端之间管路上的第三阀门、第四阀门。The third valve and the fourth valve are respectively arranged on the pipeline between the inlet of the heat exchange medium pump and the two first ends.
采用该技术方案，可通过对第一阀门、第二阀门、第三阀门、第四阀门的调控实现在不同状态下的换热介质的运行方向，保证换热介质先在吸附过程的塔中吸收热量，再循环至需要热量的脱附过程的塔中，进一步提高热量回用效率。With this technical solution, the running direction of the heat exchange medium in different states can be realized by adjusting the first valve, the second valve, the third valve, and the fourth valve, so as to ensure that the heat exchange medium is first absorbed in the tower of the adsorption process. The heat is recycled to the tower for the heat-requiring desorption process, further improving the heat recovery efficiency.
作为优选，还包括储存换热介质的容器；所述动力阀门组还包括第一三通阀和第二三通阀；Preferably, it also includes a container for storing heat exchange medium; the power valve group also includes a first three-way valve and a second three-way valve;
所述第一三通阀的三个端口分别与所述容器、换热介质泵入口、两个第一端中任一端通过管路相连；The three ports of the first three-way valve are respectively connected to the container, the inlet of the heat exchange medium pump, and any one of the two first ends through pipelines;
所述第二三通阀的三个端口分别与两组换热介质通道另一侧的两个第二端以及所述容器相连。The three ports of the second three-way valve are respectively connected to the two second ends on the other side of the two sets of heat exchange medium passages and the container.
采用上述技术方案，可通过三通阀，完成在吸附或脱附的不同状态下，换热介质的工作流向。By adopting the above technical scheme, the working flow direction of the heat exchange medium in different states of adsorption or desorption can be completed through the three-way valve.
作为优选，还包括第一换热器，所述富氧制取子系统制备的富氧空气先通过所述第一换热器与炼铁子系统排出的热风炉烟气换热，然后再进入炼铁子系统中。采用该方案进一步利用热风炉烟气的热量，提高富氧空气的温度。Preferably, it also includes a first heat exchanger, the oxygen-enriched air prepared by the oxygen-enriched production subsystem first passes through the first heat exchanger to exchange heat with the hot blast stove flue gas discharged from the ironmaking subsystem, and then enters In the ironmaking subsystem. This scheme further utilizes the heat of the hot blast stove flue gas to increase the temperature of the oxygen-enriched air.
作为进一步优选，所述炼铁子系统中热风炉排出的热风炉烟气一部分进入所述第一换热器换热，剩余部分全部进入处于脱附过程的吸/脱附塔中对脱附过程提供热量。由于对于炼铁子系统，部分热风炉烟气的热量足以对富氧空气提供预热能量，采用该技术方案，进一步提高了对热风炉烟气热量的回用。As a further preference, part of the hot blast stove flue gas discharged from the hot blast stove in the ironmaking subsystem enters the first heat exchanger for heat exchange, and the remaining part all enters the adsorption/desorption tower in the desorption process for the desorption process. Provide heat. As for the ironmaking sub-system, the heat of part of the flue gas from the hot blast stove is sufficient to provide preheating energy for the oxygen-enriched air, the adoption of this technical solution further improves the heat recovery of the flue gas from the hot blast stove.
作为优选，所述高炉系统还包括第二换热器，所述两组吸/脱附塔排出的烟气在所述第二换热器中与两组吸/脱附塔制备的富氧空气进行换热。采用该技术方案，对富氧制取子系统排出的烟气中蕴含的热量进一步回收。Preferably, the blast furnace system also includes a second heat exchanger, and the flue gas discharged from the two groups of absorption/desorption towers is mixed with the oxygen-enriched air prepared by the two groups of absorption/desorption towers in the second heat exchanger. Perform heat exchange. With this technical solution, the heat contained in the flue gas discharged from the oxygen-enriched production subsystem is further recovered.
作为进一步优选，所述两组吸/脱附塔的烟气管道分别通过两个单独的管路与烟囱和第二换热器中烟气通道入口相连，两个单独的管路上分别设有阀门。采用该技术方案，当富氧制取子系统排出的烟气温度太低时，可以直接通过阀门控制，直接排出至烟囱。此时可以通过连通温度传感器，通过温度传感器自动实现对阀门的控制。As a further preference, the flue gas pipes of the two groups of absorption/desorption towers are respectively connected to the chimney and the inlet of the flue gas passage in the second heat exchanger through two separate pipelines, and valves are respectively arranged on the two separate pipelines . With this technical solution, when the temperature of the flue gas discharged from the oxygen-enriched production subsystem is too low, it can be directly discharged to the chimney through valve control. At this time, the temperature sensor can be connected to automatically realize the control of the valve through the temperature sensor.
作为优选，所述压缩机的动力由炼铁子系统中的透平机提供。安装时，作为进一步优选，所述压缩机直接由透平机带动并与透平机同轴转动。选用该技术方案，进一步提高了能量回收效率。Preferably, the power of the compressor is provided by a turbine in the ironmaking subsystem. During installation, as a further preference, the compressor is directly driven by the turbine and rotates coaxially with the turbine. The selection of this technical solution further improves the energy recovery efficiency.
本发明变温变压耦合吸附制取富氧的方法每个吸/脱附塔都要循环进行吸附过程和脱附过程。吸附过程在常温高压下进行，放出热量。此时空气通道打开，高温烟气通道关闭，换热介质通道打开，空气中的部分氮气被吸附，含氧率提高，同时利用换热介质和空气带走吸附热；脱附过程在高温常压下进行，需要吸热。此时空气通道关闭，高温烟气通道打开，换热介质通道打开，被吸附的氮气解吸出来，吸/脱附塔重新获得吸附能力。同时脱附所需要的热量由热风炉高温烟气和换热介质共同提供。In the method for producing oxygen enriched by variable temperature and variable pressure coupling adsorption of the present invention, each absorption/desorption tower must cycle through the adsorption process and the desorption process. The adsorption process is carried out at room temperature and high pressure, releasing heat. At this time, the air channel is opened, the high-temperature flue gas channel is closed, and the heat exchange medium channel is opened. Part of the nitrogen in the air is adsorbed, and the oxygen content rate is increased. At the same time, the heat exchange medium and air are used to take away the adsorption heat; It needs to absorb heat. At this time, the air channel is closed, the high-temperature flue gas channel is opened, the heat exchange medium channel is opened, the adsorbed nitrogen is desorbed, and the adsorption/desorption tower regains its adsorption capacity. At the same time, the heat required for desorption is jointly provided by the high-temperature flue gas of the hot blast stove and the heat exchange medium.
两个吸/脱附塔间通过换热介质循环回路连通。当一塔刚开始吸附时温度高，另一塔刚开始脱附时温度低，两塔间温差大。通过换热介质循环回路，将一塔中吸附放出的热量转移到脱附状态的塔中，提供其脱附所需热量。随着吸附过程的进行，塔的温度逐渐降低；随着脱附过程的进行，塔的温度逐渐升高，两塔间温差小，换热介质无法在两塔间循环，此时换热介质从吸附塔入口进，直接从出口排出。The two absorption/desorption towers are connected through a heat exchange medium circulation loop. When one tower starts to absorb, the temperature is high, and the other tower has a low temperature when it starts to desorb, and the temperature difference between the two towers is large. Through the heat exchange medium circulation loop, the heat released by adsorption in a tower is transferred to the tower in the desorption state to provide the heat required for its desorption. With the progress of the adsorption process, the temperature of the tower gradually decreases; with the progress of the desorption process, the temperature of the tower gradually increases, the temperature difference between the two towers is small, and the heat exchange medium cannot circulate between the two towers. It enters the tower inlet and discharges directly from the outlet.
下面以两个吸/脱附塔为例，说明本发明装置的工质的工作流程。具体如下：将本发明装置的一个循环周期分为塔间回热的吸附阶段t1、塔间无回热的吸附阶段t2、塔间回热的脱附阶段t3以及塔间无回热的脱附阶段t4。Taking two absorption/desorption towers as examples below, the working process of the working medium of the device of the present invention will be described. Specifically as follows: a cycle cycle of the device of the present invention is divided into the adsorption stage t1 of the regeneration between the towers, the adsorption stage t2 without the regeneration between the towers, the desorption stage t3 of the regeneration between the towers and the desorption without the regeneration between the towers Stage t4.
塔间回热的吸附阶段t1，高温烟气通道关闭，空气通道和换热介质通道打开。空气经压缩机压缩至高压，通过压缩机出口进入处于吸附过程的吸/脱附塔中，部分氮气被吸附，空气含氧率提高，离开吸/脱附塔空气出口，经过换热器被一部分热风炉烟气加热后，进入热风炉入口。同时换热介质在吸附过程中的吸/脱附塔和脱附过程中的/脱附塔间循环流动，把吸附放出的热量携带到脱附的吸/脱附塔中加以利用。In the adsorption stage t1 of inter-tower heat recovery, the high-temperature flue gas channel is closed, and the air channel and heat exchange medium channel are opened. The air is compressed to high pressure by the compressor, enters the absorption/desorption tower in the adsorption process through the outlet of the compressor, part of the nitrogen is adsorbed, the oxygen content of the air increases, leaves the air outlet of the absorption/desorption tower, and is partially absorbed by the heat exchanger. After the hot blast stove flue gas is heated, it enters the hot blast stove inlet. At the same time, the heat exchange medium circulates between the adsorption/desorption tower during the adsorption process and the desorption/desorption tower during the desorption process, and carries the heat released by the adsorption to the desorption absorption/desorption tower for use.
塔间无回热的吸附阶段t2，高温烟气通道关闭，空气通道和换热介质通道打开。空气流动过程同t1。换热介质不在两塔间循环流动，从处于吸附过程中的吸/脱附塔换热介质入口进入，换热介质出口排出。In the adsorption stage t2 without heat recovery between the towers, the high-temperature flue gas channel is closed, and the air channel and heat exchange medium channel are opened. The air flow process is the same as t1. The heat exchange medium does not circulate between the two towers, it enters from the heat exchange medium inlet of the adsorption/desorption tower in the adsorption process, and is discharged from the heat exchange medium outlet.
塔间回热的脱附阶段t3，空气通道关闭，高温烟气通道和换热介质通道打开。传统流程中未被利用的那一部分热风炉烟气从处于脱附过程中的吸/脱附塔的烟气入口进入，在塔中放热，温度降低，然后从处于脱附过程中的吸/脱附塔的烟气出口排出，进入炼铁厂烟囱。同时换热介质在两个吸/脱附塔间循环流动，把吸附放出的热量携带到处于脱附过程的塔中加以利用。脱附热由高温烟气和循环介质共同提供。In the desorption stage t3 of inter-tower heat recovery, the air channel is closed, and the high-temperature flue gas channel and heat exchange medium channel are opened. The part of the hot blast stove flue gas that is not used in the traditional process enters from the flue gas inlet of the absorption/desorption tower in the desorption process, releases heat in the tower, and the temperature drops, and then flows from the absorption/desorption tower in the desorption process. The flue gas from the desorption tower is discharged from the outlet and enters the chimney of the ironworks. At the same time, the heat exchange medium circulates between the two adsorption/desorption towers, and carries the heat released by the adsorption to the tower in the desorption process for utilization. The heat of desorption is jointly provided by high-temperature flue gas and circulating medium.
塔间无回热的脱附阶段t4，空气通道关闭，高温烟气通道和换热介质通道打开。高温烟气流动过程同t3。换热介质不在两塔间循环流动。所需脱附热由高温烟气单独提供。In the desorption stage t4 without heat recovery between the towers, the air channel is closed, and the high-temperature flue gas channel and the heat exchange medium channel are opened. The high temperature flue gas flow process is the same as t3. The heat exchange medium does not circulate between the two towers. The required desorption heat is provided by high temperature flue gas alone.
本发明与传统的炼铁工艺流程相比，更充分的利用系统的余热余压能源，具有以下有益效果：Compared with the traditional ironmaking process flow, the present invention makes full use of the waste heat and pressure energy of the system, and has the following beneficial effects:
(1)利用热风炉烟气余热制取富氧空气原料，更具节能减排效果。热风炉烟气用于加热原料气，同时用于制取富氧空气，不但提高了余热的回收利用率，而且减少了高炉的焦炭消耗和提高了生铁产量。(1) The raw material of oxygen-enriched air is produced by using the waste heat of the flue gas of the hot blast stove, which has more energy-saving and emission-reducing effects. The hot stove flue gas is used to heat the raw material gas and to produce oxygen-enriched air at the same time, which not only improves the recovery and utilization rate of waste heat, but also reduces the coke consumption of the blast furnace and increases the pig iron production.
(2)采用透平机-压缩机复合装置压缩原料气，减少能量形式转换。充分利用高炉煤气余压，通过透平机-压缩机复合装置压缩原料气，去除了机械能与电能的两次转化过程，提高了余压的回收利用效率。(2) The raw material gas is compressed by a turbine-compressor composite device to reduce energy form conversion. By making full use of the residual pressure of blast furnace gas, the raw material gas is compressed through a turbine-compressor composite device, which eliminates the two conversion processes of mechanical energy and electrical energy, and improves the recovery and utilization efficiency of residual pressure.
(3)采用塔间回热的变温变压耦合吸附工艺，进一步提高了余热的回收利用率。高温常压脱附，常温高压吸附，可减少吸附剂的使用量。并采用塔间回热，减少热风炉烟气消耗和强化吸脱附过程的传热传质。(3) The variable temperature and pressure coupled adsorption process of inter-tower heat recovery is adopted to further improve the recovery and utilization rate of waste heat. High temperature and normal pressure desorption, normal temperature and high pressure adsorption, can reduce the amount of adsorbent used. In addition, inter-tower heat recovery is adopted to reduce the consumption of flue gas from the hot blast stove and enhance the heat and mass transfer in the process of adsorption and desorption.
附图说明Description of drawings
图1为传统高炉系统的结构图；Fig. 1 is a structural diagram of a traditional blast furnace system;
图2为本发明的利用余热余压自供富氧空气的节能高炉系统的结构示意图；Fig. 2 is the structural representation of the energy-saving blast furnace system of the present invention utilizing waste heat and pressure to self-supply oxygen-enriched air;
图3为本发明的利用余热余压自供富氧空气的节能高炉系统的详细结构示意图。Fig. 3 is a schematic diagram of the detailed structure of an energy-saving blast furnace system for self-supplying oxygen-enriched air by utilizing waste heat and pressure of the present invention.
其中：in:
1为热风炉；2为高炉；3为除尘装置；4为透平机；5为热风炉入口处的第一换热器；6为吸附塔出口的第二换热器；7为第一吸/脱附塔；8为压缩机；9为第二吸/脱附塔；10为换热介质泵。1 is the hot blast stove; 2 is the blast furnace; 3 is the dust removal device; 4 is the turbine; 5 is the first heat exchanger at the entrance of the hot blast stove; 6 is the second heat exchanger at the outlet of the adsorption tower; 7 is the first suction /desorption tower; 8 is a compressor; 9 is a second absorption/desorption tower; 10 is a heat exchange medium pump.
1a为热风炉的高炉煤气入口；1b为热风炉的高温富氧空气出口；1c为热风炉的热风炉烟气出口；1d为热风炉的富氧空气入口；2a为高炉的富氧空气入口；2b为高炉的高炉煤气出口；3a为除尘装置的入口；3b为除尘装置的出口；4a为透平机的入口；4b为透平机的出口；5a为第一换热器的高温烟气入口；5b为第一换热器的富氧空气出口；5c为第一换热器的高温烟气出口；5d为第一换热器的空气入口；6a为第二换热器的高温烟气出口；6b为第二换热器的高温烟气入口；6c为第二换热器的空气出口；6d为第二换热器的空气入口；7a为第一吸/脱附塔7的空气出口；7b为第一吸/脱附塔7的空气入口；7c为第一吸/脱附塔7的高温烟气入口；7d为第一吸/脱附塔7的高温烟气出口；7e为第一吸/脱附塔7的换热介质出口；7f为第一吸/脱附塔7的换热介质入口；8a为压缩机的排气口；8b为压缩机的空气入口；9a为第二吸/脱附塔9的空气出口；9b为第二吸/脱附塔9的空气入口；9c为第二吸/脱附塔9的高温烟气入口；9d为第二吸/脱附塔9的高温烟气出口；9e为第二吸/脱附塔9的换热介质出口；9f为第二吸/脱附塔9的换热介质入口；10a为换热介质泵的入口；10b为换热介质泵的出口。1a is the blast furnace gas inlet of the hot blast stove; 1b is the high temperature oxygen-enriched air outlet of the hot blast stove; 1c is the hot blast stove flue gas outlet of the hot blast stove; 1d is the oxygen-enriched air inlet of the hot blast stove; 2a is the oxygen-enriched air inlet of the blast furnace; 2b is the blast furnace gas outlet of the blast furnace; 3a is the inlet of the dust removal device; 3b is the outlet of the dust removal device; 4a is the inlet of the turbine; 4b is the outlet of the turbine; 5a is the high-temperature flue gas inlet of the first heat exchanger ; 5b is the oxygen-enriched air outlet of the first heat exchanger; 5c is the high-temperature flue gas outlet of the first heat exchanger; 5d is the air inlet of the first heat exchanger; 6a is the high-temperature flue gas outlet of the second heat exchanger ; 6b is the high-temperature flue gas inlet of the second heat exchanger; 6c is the air outlet of the second heat exchanger; 6d is the air inlet of the second heat exchanger; 7a is the air outlet of the first absorption/desorption tower 7; 7b is the air inlet of the first absorption/desorption tower 7; 7c is the high-temperature flue gas inlet of the first absorption/desorption tower 7; 7d is the high-temperature flue gas outlet of the first absorption/desorption tower 7; 7e is the first The heat exchange medium outlet of the absorption/desorption tower 7; 7f is the heat exchange medium inlet of the first absorption/desorption tower 7; 8a is the exhaust port of the compressor; 8b is the air inlet of the compressor; 9a is the second suction 9b is the air inlet of the second absorption/desorption tower 9; 9c is the high-temperature flue gas inlet of the second absorption/desorption tower 9; 9d is the air inlet of the second absorption/desorption tower 9 High-temperature flue gas outlet; 9e is the heat exchange medium outlet of the second absorption/desorption tower 9; 9f is the heat exchange medium inlet of the second absorption/desorption tower 9; 10a is the heat exchange medium pump inlet; 10b is the heat exchange medium Outlet of the medium pump.
具体实施方式Detailed ways
如图2所示，一种基于变温变压耦合吸附的利用余热余压自供富氧空气的节能高炉系统，由传统炼铁子系统以及富氧制取子系统组成。As shown in Figure 2, an energy-saving blast furnace system based on variable temperature and pressure coupled adsorption that uses waste heat and pressure to self-supply oxygen-enriched air consists of a traditional ironmaking subsystem and an oxygen-enriched production subsystem.
传统炼铁子系统由热风炉1、高炉2、除尘装置3、透平机4、热风炉进口处的第一换热器5组成；The traditional ironmaking subsystem consists of a hot blast stove 1, a blast furnace 2, a dust removal device 3, a turbine 4, and a first heat exchanger 5 at the inlet of the hot blast stove;
富氧制取子系统由吸附塔后的第二换热器6、第一吸/脱附塔7、压缩机8、第二吸/脱附塔9以及换热介质泵10组成。The oxygen enrichment production subsystem consists of the second heat exchanger 6 after the adsorption tower, the first absorption/desorption tower 7 , the compressor 8 , the second absorption/desorption tower 9 and the heat exchange medium pump 10 .
上述各部件的连接关系如下：The connections of the above components are as follows:
热风炉1的富氧空气出口1b与高炉2的富氧空气入口2a相连；高炉2的高炉煤气出口2b与除尘装置3的入口3a相连；除尘装置3的出口3b与透平机4的入口4a相连；高炉煤气在透平机4中输出功后经过透平机4的出口4b与热风炉1的高炉煤气入口1a相连，回到热风炉1燃烧，对热风炉1内的富氧空气进行加热；热风炉1的热风炉烟气出口1c与第一换热器5的高温烟气入口5a相连；第一换热器5的富氧空气出口5b和热风炉1的富氧空气入口1d相连；从热风炉1出来的一部分烟气经过第一换热器5的高温烟气出口5c排出，剩余的烟气分别进入第一吸/脱附塔7、第二吸/脱附塔9；第二换热器6的空气出口6c和第一换热器5的空气入口5d直接相连；第一吸/脱附塔7的空气出口7a和第二换热器6的空气入口6d相连；大气压下的空气从压缩机8的空气入口8b进入，从压缩机8的排气口8a排出，再由第一吸/脱附塔7的空气入口7b进入塔中进行吸/脱附过程；热风炉1的热风炉烟气出口1c和第一吸/脱附塔7的高温烟气入口7c相连；第一吸/脱附塔7的高温烟气出口7d和第二换热器6的高温烟气入口6b相连，再经第二换热器6的高温烟气出口6a送到烟囱；脱附塔的空气入口9b和压缩机的排气口8a相连；第二吸/脱附塔9的空气出口9a和第二换热器6的空气入口6d相连；第二吸/脱附塔9的空气入口9b与压缩机8的排气口8a相连；第二吸/脱附塔9的高温烟气入口9c和热风炉1的热风炉烟气出口1c相连；第二吸/脱附塔9的高温烟气出口9d和第二换热器6的高温烟气入口6b相连。The oxygen-enriched air outlet 1b of the hot blast stove 1 is connected to the oxygen-enriched air inlet 2a of the blast furnace 2; the blast furnace gas outlet 2b of the blast furnace 2 is connected to the inlet 3a of the dust removal device 3; the outlet 3b of the dust removal device 3 is connected to the inlet 4a of the turbine 4 connected; the blast furnace gas is connected to the blast furnace gas inlet 1a of the hot blast stove 1 through the outlet 4b of the turbine 4 after outputting work in the turbine 4, returns to the hot blast stove 1 for combustion, and heats the oxygen-enriched air in the hot blast stove 1 The hot blast stove flue gas outlet 1c of the hot blast stove 1 links to each other with the high-temperature flue gas inlet 5a of the first heat exchanger 5; the oxygen-enriched air outlet 5b of the first heat exchanger 5 links to each other with the oxygen-enriched air inlet 1d of the hot blast stove 1; Part of the flue gas coming out from the hot blast stove 1 is discharged through the high-temperature flue gas outlet 5c of the first heat exchanger 5, and the remaining flue gas enters the first absorption/desorption tower 7 and the second absorption/desorption tower 9 respectively; The air outlet 6c of the heat exchanger 6 is directly connected with the air inlet 5d of the first heat exchanger 5; the air outlet 7a of the first absorption/desorption tower 7 is connected with the air inlet 6d of the second heat exchanger 6; Air enters from the air inlet 8b of compressor 8, discharges from the exhaust port 8a of compressor 8, and enters in the tower by the air inlet 7b of the first absorption/desorption tower 7 to carry out the absorption/desorption process; The flue gas outlet 1c of the hot blast stove is connected to the high-temperature flue gas inlet 7c of the first absorption/desorption tower 7; the high-temperature flue gas outlet 7d of the first absorption/desorption tower 7 is connected to the high-temperature flue gas inlet 6b of the second heat exchanger 6 connected, and sent to the chimney through the high-temperature flue gas outlet 6a of the second heat exchanger 6; the air inlet 9b of the desorption tower is connected with the exhaust port 8a of the compressor; the air outlet 9a of the second absorption/desorption tower 9 and The air inlet 6d of the second heat exchanger 6 links to each other; the air inlet 9b of the second absorption/desorption tower 9 links to each other with the exhaust port 8a of compressor 8; the high-temperature flue gas inlet 9c of the second absorption/desorption tower 9 and The hot blast stove flue gas outlet 1c of the hot blast stove 1 is connected; the high temperature flue gas outlet 9d of the second absorption/desorption tower 9 is connected with the high temperature flue gas inlet 6b of the second heat exchanger 6 .
换热介质系统：换热介质从换热介质泵10的入口10a进入，经换热介质泵10的出口10b流出；换热介质泵10的出口10b和第一吸/脱附塔7的换热介质入口7f或第二吸/脱附塔9的换热介质入口9f相连；第一吸/脱附塔7的换热介质出口7e或第二吸/脱附塔9的换热介质出口9e连通，同时分别通过管路与换热介质泵10的入口10a相连。Heat exchange medium system: the heat exchange medium enters from the inlet 10a of the heat exchange medium pump 10 and flows out through the outlet 10b of the heat exchange medium pump 10; the heat exchange between the outlet 10b of the heat exchange medium pump 10 and the first absorption/desorption tower 7 The medium inlet 7f or the heat exchange medium inlet 9f of the second absorption/desorption tower 9 are connected; the heat exchange medium outlet 7e of the first absorption/desorption tower 7 or the heat exchange medium outlet 9e of the second absorption/desorption tower 9 are connected , and are respectively connected to the inlet 10a of the heat exchange medium pump 10 through pipelines.
同时还设置了阀门A、阀门B、阀门C、阀门D、阀门E、阀门F、阀门G、阀门H、阀门I、阀门J、阀门K、阀门L、阀门M、阀门N。其中阀门B和阀门L为三通阀。阀门B的三个开口分别定义为第一端、第二端、第三端。阀门B的第二端通过管路与第一吸/脱附塔7换热介质入口7f连通，该管路上设置有上述的阀门A。阀门B的第三端通过管路与第二吸/脱附塔9的换热介质入口9f的连通，该管路上设置有上述的阀门C，同时换热介质泵10也设置在该管路上，换热介质泵10设置在阀门B的第三端与阀门C之间的管路上。同时在换热介质泵10的出口10b与第一吸/脱附塔7换热介质入口7f之间设置管路，该管路上设有上述的阀门D；另外在第二吸/脱附塔9的换热介质入口9f与换热介质泵10的入口10a之间设置管路，该管路上设置有上述的阀门E。压缩机8的排气口8a与第一吸/脱附塔7的空气入口7b之间的管路上设置有上述的阀门F；压缩机8的排气口8a与第二吸/脱附塔9的空气入口9b之间的管路上设置有上述的阀门G。第一吸/脱附塔7的高温烟气出口7d和第二吸/脱附塔9的高温烟气出口9d与烟囱之间也设置了管路，该管路上设置有上述的阀门H，当从第一吸/脱附塔7的高温烟气出口7d和第二吸/脱附塔9的高温烟气出口9d出来的烟气温度比较低时，不需要通过第二换热器6回收热量，此时阀门H开启，烟气可直接通过该管路排出至烟囱中。第一吸/脱附塔7的高温烟气出口7d和第二吸/脱附塔9的高温烟气出口9d与第二换热器6的高温烟气入口6b之间的管路设置有上述的阀门I。第一吸/脱附塔7的空气出口7a与第二换热器6的空气入口6d之间的管路上设有上述的阀门J；第二吸/脱附塔9的空气出口9a与第二换热器6的空气入口6d之间的管路上设有上述的阀门K。第一吸/脱附塔7的换热介质出口7e、第二吸/脱附塔9的换热介质出口9e、阀门B的入口之间设有上述的阀门L；阀门L的三个开口分别定义为第一端、第二端和第三端，阀门L的第一端与阀门B的第一端连通，两者之间一般设置有储存换热介质的容器，换热介质一般为水，用于吸收吸附过程中的热量，同时将吸附产生的热量回用至脱附过程中。阀门L的第二端通过管路与上述的第一吸/脱附塔7的换热介质出口7e连通。阀门L的第三端通过管路与上述的第二吸/脱附塔9的换热介质出口9e连通。At the same time, valve A, valve B, valve C, valve D, valve E, valve F, valve G, valve H, valve I, valve J, valve K, valve L, valve M, and valve N are also set. Among them, valve B and valve L are three-way valves. The three openings of the valve B are respectively defined as a first end, a second end, and a third end. The second end of the valve B communicates with the heat exchange medium inlet 7f of the first absorption/desorption tower 7 through a pipeline, and the above-mentioned valve A is arranged on the pipeline. The third end of the valve B communicates with the heat exchange medium inlet 9f of the second absorption/desorption tower 9 through a pipeline, the above-mentioned valve C is arranged on the pipeline, and the heat exchange medium pump 10 is also arranged on the pipeline, The heat exchange medium pump 10 is arranged on the pipeline between the third end of the valve B and the valve C. At the same time, a pipeline is set between the outlet 10b of the heat exchange medium pump 10 and the heat exchange medium inlet 7f of the first absorption/desorption tower 7, and the above-mentioned valve D is arranged on the pipeline; in addition, in the second absorption/desorption tower 9 A pipeline is provided between the heat exchange medium inlet 9f of the heat exchange medium pump 10 and the inlet 10a of the heat exchange medium pump 10, and the above-mentioned valve E is provided on the pipeline. Above-mentioned valve F is arranged on the pipeline between the exhaust port 8a of compressor 8 and the air inlet 7b of the first absorption/desorption tower 7; The above-mentioned valve G is arranged on the pipeline between the air inlets 9b. A pipeline is also arranged between the high-temperature flue gas outlet 7d of the first absorption/desorption tower 7 and the high-temperature flue gas outlet 9d of the second absorption/desorption tower 9 and the chimney, and the above-mentioned valve H is arranged on the pipeline. When the flue gas temperature from the high-temperature flue gas outlet 7d of the first absorption/desorption tower 7 and the high-temperature flue gas outlet 9d of the second absorption/desorption tower 9 is relatively low, there is no need to recover heat through the second heat exchanger 6 , at this time the valve H is opened, and the flue gas can be directly discharged into the chimney through the pipeline. The pipeline between the high-temperature flue gas outlet 7d of the first absorption/desorption tower 7 and the high-temperature flue gas outlet 9d of the second absorption/desorption tower 9 and the high-temperature flue gas inlet 6b of the second heat exchanger 6 is provided with the above-mentioned The valve I. Above-mentioned valve J is arranged on the pipeline between the air outlet 7a of the first absorption/desorption tower 7 and the air inlet 6d of the second heat exchanger 6; The above-mentioned valve K is provided on the pipeline between the air inlets 6d of the heat exchanger 6 . The above-mentioned valve L is arranged between the heat exchange medium outlet 7e of the first absorption/desorption tower 7, the heat exchange medium outlet 9e of the second absorption/desorption tower 9, and the inlet of the valve B; the three openings of the valve L are respectively It is defined as the first end, the second end and the third end. The first end of the valve L communicates with the first end of the valve B. There is generally a container for storing the heat exchange medium between the two. The heat exchange medium is generally water. It is used to absorb the heat in the adsorption process, and at the same time reuse the heat generated by the adsorption to the desorption process. The second end of the valve L communicates with the heat exchange medium outlet 7e of the above-mentioned first absorption/desorption tower 7 through a pipeline. The third end of the valve L communicates with the heat exchange medium outlet 9e of the above-mentioned second absorption/desorption tower 9 through a pipeline.
吸附过程在常温高压下进行，放出热量。此时空气通道打开，高温烟气通道关闭，换热介质通道打开，空气中的部分氮气被吸附，含氧率提高，同时利用换热介质和空气带走吸附热；脱附过程在高温常压下进行，需要吸热。此时空气通道关闭，高温烟气通道打开，换热介质通道打开，被吸附的氮气解吸出来，吸附塔重新获得吸附能力。同时脱附所需要的热量由热风炉高温烟气和换热介质共同提供。The adsorption process is carried out at room temperature and high pressure, releasing heat. At this time, the air channel is opened, the high-temperature flue gas channel is closed, and the heat exchange medium channel is opened. Part of the nitrogen in the air is adsorbed, and the oxygen content rate is increased. At the same time, the heat exchange medium and air are used to take away the adsorption heat; It needs to absorb heat. At this time, the air channel is closed, the high-temperature flue gas channel is opened, the heat exchange medium channel is opened, the adsorbed nitrogen is desorbed, and the adsorption tower regains its adsorption capacity. At the same time, the heat required for desorption is jointly provided by the high-temperature flue gas of the hot blast stove and the heat exchange medium.
第一吸/脱附塔7、第二吸/脱附塔9交替的作为吸附塔和脱附塔使用，以第一吸/脱附塔7作为吸附塔，第二吸/脱附塔9作为脱附塔使用为例，说明第一吸/脱附塔7、第二吸/脱附塔9的工作过程：The first absorption/desorption tower 7, the second absorption/desorption tower 9 alternately use as adsorption tower and desorption tower, with the first absorption/desorption tower 7 as adsorption tower, the second absorption/desorption tower 9 as The use of the desorption tower is taken as an example to illustrate the working process of the first absorption/desorption tower 7 and the second absorption/desorption tower 9:
热风炉1的高温烟气进入第二吸/脱附塔9中提供脱附过程所需热量(脱附过程中脱附塔的温度逐渐升高，使得脱附过程前阶段放热后的烟气温度低，脱附过程后阶段放热后的烟气温度高)。出口烟气温度高时，阀门I打开，阀门H关闭，烟气与第一吸/脱附塔7空气出口7a的富氧空气在第二换热器6内换热，以进一步利用废热；出口烟气温度低，阀门H打开，阀门I关闭，烟气直接经过阀门H送至烟囱。此过程此设计使得系统的能量利用率进一步提高，实际安装过程中，可根据需要设置温度传感器等，阀门H和阀门I可设置为受温度传感器控制的电控阀等。The high-temperature flue gas of the hot blast stove 1 enters the second absorption/desorption tower 9 to provide the heat required for the desorption process (the temperature of the desorption tower gradually increases during the desorption process, so that the flue gas after the heat release in the previous stage of the desorption process The temperature is low, and the temperature of the flue gas after the exothermic stage of the desorption process is high). When the outlet flue gas temperature is high, valve I is opened and valve H is closed, and the flue gas exchanges heat with the oxygen-enriched air at the air outlet 7a of the first absorption/desorption tower 7 in the second heat exchanger 6 to further utilize waste heat; The flue gas temperature is low, the valve H is opened, the valve I is closed, and the flue gas is directly sent to the chimney through the valve H. The design of this process further improves the energy utilization rate of the system. In the actual installation process, temperature sensors can be set as required. Valve H and valve I can be set as electronically controlled valves controlled by temperature sensors.
第一吸/脱附塔7吸附初期(即第二吸/脱附塔9脱附初期)，两塔间温差大，采用塔间回热的方案，将吸附塔(第一吸/脱附塔7)中放出的热量转移到脱附塔(第二吸/脱附塔9)中，提供其脱附所需热量，称为有回热的吸脱附过程；第一吸/脱附塔7吸附后期(即第二吸/脱附塔9脱附后期)，两塔间温差缩小，不需要采用塔间回热的方案，称为无回热的吸脱附过程。此设计也可以进一步提高系统的能量利用效果。The first absorption/desorption tower 7 initial stages of adsorption (i.e. the second absorption/desorption tower 9 desorption initial stages), the temperature difference between the two towers is large, adopt the scheme of reheating between the towers, and the adsorption tower (the first absorption/desorption tower 9) 7) The heat released in the process is transferred to the desorption tower (the second absorption/desorption tower 9) to provide the required heat for its desorption, which is called the absorption and desorption process with regenerative heat; the first absorption/desorption tower 7 In the late stage of adsorption (that is, the late stage of desorption in the second adsorption/desorption tower 9), the temperature difference between the two towers is reduced, and there is no need to adopt the scheme of reheating between towers, which is called the adsorption-desorption process without regenerative heat. This design can also further improve the energy utilization effect of the system.
有回热的吸脱附过程：(1)第一吸/脱附塔7中吸附，第二吸/脱附塔9中脱附：阀门D、阀门L、阀门E打开，阀门A、阀门C关闭，阀门B的第一端和第三端在初期阶段导通，保证换热介质进入，换热介质完成一个循环后，阀门B关闭。换热介质依次经过阀门B的第一端和第三端、换热介质泵10的入口10a、换热介质泵10的出口10b、阀门D、第一吸/脱附塔7的换热介质入口7f、第一吸/脱附塔7的换热介质出口7e、阀门L的第三端和第二端、第二吸/脱附塔9的换热介质出口9e(此时作为换热介质入口使用)、第二吸/脱附塔9的换热介质入口9f(此时作为换热介质出口使用)、阀门E，最终回到换热介质泵10的入口10a，完成一次循环；(2)第一吸/脱附塔7脱附，第二吸/脱附塔9吸附：阀门B、阀门C、阀门L、阀门A打开，阀门D、阀门E关闭，阀门B的第二端和第三端导通。换热介质依次换热介质泵10的出口10b、阀门C、第二吸/脱附塔9的换热介质入口9f、第二吸/脱附塔9的换热介质出口9e、阀门L的第三端和第二端、第一吸/脱附塔7的换热介质出口7e(此时作为换热介质入口使用)、第一吸/脱附塔7的换热介质入口7f(此时作为换热介质出口使用)、阀门A、阀门B的第二端和第三端，最后回到换热介质泵10的入口10a；Adsorption and desorption process with heat recovery: (1) Adsorption in the first absorption/desorption tower 7, desorption in the second absorption/desorption tower 9: valve D, valve L, valve E open, valve A, valve C Closed, the first end and the third end of valve B are turned on at the initial stage to ensure that the heat exchange medium enters, and after the heat exchange medium completes a cycle, valve B is closed. The heat exchange medium sequentially passes through the first end and the third end of the valve B, the inlet 10a of the heat exchange medium pump 10, the outlet 10b of the heat exchange medium pump 10, the valve D, and the heat exchange medium inlet of the first absorption/desorption tower 7 7f, the heat exchange medium outlet 7e of the first absorption/desorption tower 7, the third end and the second end of the valve L, the heat exchange medium outlet 9e of the second absorption/desorption tower 9 (at this time as the heat exchange medium inlet use), the heat exchange medium inlet 9f of the second absorption/desorption tower 9 (used as the heat exchange medium outlet at this time), the valve E, finally returns to the inlet 10a of the heat exchange medium pump 10, and completes a cycle; (2) The first absorption/desorption tower 7 desorbs, the second absorption/desorption tower 9 absorbs: valve B, valve C, valve L, valve A are opened, valve D, valve E are closed, the second end of valve B and the third end terminal conduction. The heat exchange medium is followed by the outlet 10b of the heat exchange medium pump 10, the valve C, the heat exchange medium inlet 9f of the second absorption/desorption tower 9, the heat exchange medium outlet 9e of the second absorption/desorption tower 9, and the first valve L of the valve L. Three ends and the second end, the heat exchange medium outlet 7e of the first absorption/desorption tower 7 (used as the heat exchange medium inlet at this time), the heat exchange medium inlet 7f of the first absorption/desorption tower 7 (used as the heat exchange medium inlet at this time) The heat exchange medium outlet is used), the valve A, the second end and the third end of the valve B, and finally return to the inlet 10a of the heat exchange medium pump 10;
无回热的吸脱附过程：(1)第一吸/脱附塔7吸附，第二吸/脱附塔9脱附：阀门B的第一端和第三端导通、阀门D打开、阀门L的第二端和第一端导通，阀门A、阀门C、阀门E关闭。换热介质依次经过阀门B的第一端和第三端导通、换热介质泵10的入口10a、换热介质泵10的出口10b、阀门D、第一吸/脱附塔7的换热介质入口7f、第一吸/脱附塔7的换热介质出口7e、阀门L的第二端和第一端最终回到储存换热介质的容器；(2)第一吸/脱附塔7脱附，第二吸/脱附塔9吸附：阀门B的第一端和第三端导通、阀门C打开、阀门L的第三端和第一端导通，阀门A、阀门D、阀门E关闭。换热介质依次经过阀门B的第一端和第三端、换热介质泵10的入口10a、换热介质泵10的出口10b、阀门C、第二吸/脱附塔9的换热介质入口9f、第二吸/脱附塔9的换热介质出口9e、阀门L的第三端和第一端，最终回到储存换热介质的容器。Absorption and desorption process without heat recovery: (1) Adsorption in the first absorption/desorption tower 7, desorption in the second absorption/desorption tower 9: the first end of the valve B and the third end are connected, the valve D is opened, The second end of the valve L is connected to the first end, and the valves A, C, and E are closed. The heat exchange medium is conducted through the first end and the third end of the valve B, the inlet 10a of the heat exchange medium pump 10, the outlet 10b of the heat exchange medium pump 10, the valve D, and the heat exchange of the first absorption/desorption tower 7 The medium inlet 7f, the heat exchange medium outlet 7e of the first absorption/desorption tower 7, the second end and the first end of the valve L finally return to the container for storing the heat exchange medium; (2) the first absorption/desorption tower 7 Desorption, second adsorption/desorption tower 9 adsorption: the first end of valve B is connected to the third end, valve C is opened, the third end of valve L is connected to the first end, valve A, valve D, valve E off. The heat exchange medium passes through the first end and the third end of the valve B, the inlet 10a of the heat exchange medium pump 10, the outlet 10b of the heat exchange medium pump 10, the valve C, and the heat exchange medium inlet of the second absorption/desorption tower 9 9f, the heat exchange medium outlet 9e of the second absorption/desorption tower 9, the third end and the first end of the valve L, and finally return to the container for storing the heat exchange medium.
当第一吸/脱附塔7吸附、第二吸/脱附塔9脱附时，阀门F和阀门J打开；阀门K和阀门G关闭；当第一吸/脱附塔7脱附、第二吸/脱附塔9吸附时，阀门K和阀门G打开，阀门F和阀门J关闭。阀门M、阀门N分别用于控制第一吸/脱附塔7、第二吸/脱附塔9内高温烟气通道的导通。When the first absorption/desorption tower 7 is adsorbed and the second absorption/desorption tower 9 is desorbed, valve F and valve J are opened; valve K and valve G are closed; when the first absorption/desorption tower 7 is desorbed, the second When the second absorption/desorption tower 9 is adsorbing, valve K and valve G are opened, and valve F and valve J are closed. The valve M and the valve N are respectively used to control the conduction of the high-temperature flue gas channels in the first absorption/desorption tower 7 and the second absorption/desorption tower 9 .
性能分析：以一个生铁产量为100吨/小时的高炉炼铁系统为例，高炉容积为1000m3。热风炉烟气温度和压强分别为400℃和0.12MPa(压强略高于大气压，以便排出烟囱)，热风炉烟气流量为：250000标方/小时。高炉煤气温度和压力分别为200℃和0.35MPa，高炉煤气流量为：150000标方/小时。富氧空气富氧率为3％(即空气中含氧率为24％)，鼓风量为100000标方/小时。Performance analysis: Take a blast furnace ironmaking system with a pig iron output of 100 tons/hour as an example, and the volume of the blast furnace is 1000m 3 . The temperature and pressure of the flue gas from the hot blast stove are 400°C and 0.12MPa respectively (the pressure is slightly higher than atmospheric pressure so as to be discharged from the chimney). The blast furnace gas temperature and pressure are 200°C and 0.35MPa respectively, and the blast furnace gas flow rate is 150,000 standard cubic meters per hour. The oxygen enrichment rate of the oxygen-enriched air is 3% (that is, the oxygen content rate in the air is 24%), and the blast volume is 100,000 standard cubic meters per hour.
吸附塔中工作状态：温度和压强分别为30℃和0.35MPa，即常温高压下吸附；脱附塔中工作状态：温度和压强分别为400℃和0.1MPa，即高温常压下脱附。两塔工作状态每两小时切换一次。Working state in the adsorption tower: temperature and pressure are 30°C and 0.35MPa respectively, that is, adsorption at normal temperature and high pressure; working state in the desorption tower: temperature and pressure are 400°C and 0.1MPa, that is, desorption at high temperature and normal pressure. The working status of the two towers is switched every two hours.
经过查阅相关的国家标准和计算，透平机和压缩机的绝热压缩效率取0.9。吸附塔中分子筛以10元/kg计算，系统分子筛投资成本为556万元，两个吸附塔及系统管道设备初投资与分子筛成本相近，约为556万元。分子筛使用年限为5年，吸附塔及管道设备使用年限为10年。压缩机和透平机参考市场价估算，初投资成本约为1130万元，使用年限均为10年。将系统的部分计算参数列出，结果如表1：After reviewing relevant national standards and calculations, the adiabatic compression efficiency of the turbine and compressor is taken as 0.9. The molecular sieve in the adsorption tower is calculated at 10 yuan/kg, and the investment cost of the system molecular sieve is 5.56 million yuan. The initial investment of the two adsorption towers and system piping equipment is similar to the molecular sieve cost, about 5.56 million yuan. The service life of the molecular sieve is 5 years, and the service life of the adsorption tower and pipeline equipment is 10 years. The compressor and turbine are estimated with reference to the market price. The initial investment cost is about 11.3 million yuan, and the service life is 10 years. List some calculation parameters of the system, the results are shown in Table 1:
表1Table 1
将本系统和原系统进行对比，对比结果如表2：Comparing this system with the original system, the comparison results are shown in Table 2:
表2Table 2
由表2可知，总成本增加：556+1686-1036＝1206万元，富氧后本系统每年多产生的净收益为：1002-306＝696万元；收回成本年限：2年。同时本发明利用炼铁厂多余的热风炉烟气热量和高炉煤气的余压能量来制取富氧，可以提高生铁产量大约每年87.2万吨，减少燃料消耗成本约910.4万元。本系统更为直接充分地利用了炼铁厂余热余压能量，有效地起到了节能减排效果，并且兼具较好的经济效益。It can be seen from Table 2 that the total cost increases: 556+1686-1036=12.06 million yuan, and the net income generated by the system after oxygen enrichment is: 1002-306=6.96 million yuan; the cost recovery period: 2 years. At the same time, the present invention utilizes excess hot blast stove flue gas heat and blast furnace gas residual pressure energy in ironworks to produce oxygen enrichment, which can increase pig iron production by approximately 872,000 tons per year and reduce fuel consumption costs by approximately 9.104 million yuan. This system more directly and fully utilizes the waste heat and pressure energy of the ironworks, effectively achieves the effect of energy saving and emission reduction, and has good economic benefits.
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