技术领域technical field
本发明涉及一种固定床气化生产1.0～2.2MPa水煤气的方法，属于煤炭、焦炭化工气化领域。The invention relates to a fixed-bed gasification method for producing 1.0-2.2 MPa water gas, which belongs to the field of coal and coke chemical gasification.
背景技术Background technique
煤气化反应是发生在碳和载氧的气化剂(O2、H2O、CO2)之间的一种化学反应。水煤气用途非常广泛，其主要成份为氢气和一氧化碳，过去主要用作燃气，现在主要用于制备化工产品，如作为生产甲醇、乙二醇、多元醇、醋酸、合成氨、联碱等的原料气。Coal gasification reaction is a chemical reaction between carbon and oxygen-carrying gasification agent (O2 , H2 O, CO2 ). Water gas is widely used. Its main components are hydrogen and carbon monoxide. It was mainly used as gas in the past, but now it is mainly used to prepare chemical products, such as raw material gas for the production of methanol, ethylene glycol, polyols, acetic acid, synthetic ammonia, and combined alkali.
煤气化技术的发展历史已有100多年，气化炉类型先后也有近百种，我国也十分重视煤气化技术的研究与开发，依靠自身科技实力研发出多种固定床、流化床及气流床气化技术。然而，目前国内的中小型化肥企业、冶炼厂、金属加工厂、铸造厂、陶瓷厂、玻璃厂等多数仍采用老式的煤气化炉，即固定床常压间歇炉，使用时煤气需要加压，电耗较高，并且该工艺生产效率低、原料转化率低、灰渣残炭高、安全隐患多，致使企业生产成本升高，而经济效益降低。The development history of coal gasification technology has been more than 100 years, and there are nearly a hundred types of gasifiers. my country also attaches great importance to the research and development of coal gasification technology, and has developed a variety of fixed beds, fluidized beds and entrained beds relying on its own scientific and technological strength. gasification technology. However, at present, most domestic small and medium-sized chemical fertilizer enterprises, smelters, metal processing plants, foundries, ceramic factories, glass factories, etc. still use old-fashioned coal gasification furnaces, that is, fixed-bed atmospheric pressure intermittent furnaces, and the gas needs to be pressurized when used. The power consumption is high, and the process has low production efficiency, low raw material conversion rate, high ash residual carbon, and many safety hazards, which lead to increased production costs and reduced economic benefits.
为提高经济效益，我国先后于20世纪50年代引进温克勒流化床技术，70年代引进鲁奇固定床气化技术，80年代引进德士古加压水煤浆气化技术，90年代引进壳牌煤粉气化技术等。但是每种煤气化技术都有自身的适应性和局限性，如不同的原料来源需对应不同的炉型等。并且国外的气化炉大多数仅适用于大型化工生产企业，前期投资较大，一般企业难以承受。In order to improve economic benefits, my country successively introduced Winkler fluidized bed technology in the 1950s, Lurgi fixed bed gasification technology in the 1970s, Texaco pressurized coal-water slurry gasification technology in the 1980s, and Shell pulverized coal gasification technology, etc. However, each coal gasification technology has its own adaptability and limitations, such as different raw material sources corresponding to different furnace types, etc. Moreover, most foreign gasifiers are only suitable for large-scale chemical production enterprises, and the initial investment is relatively large, which is difficult for ordinary enterprises to bear.
为调节气体成分，中小型化肥生产企业均设置有一氧化碳变换工序，变换压力主要有0.8～1.0MPa、2.0～2.2MPa两种，而间歇炉生产的常压水煤气必须利用煤气压缩机加压到上述压力才能使用，因此需要消耗大量的电能，电耗费用占合成氨成本的近30％，不利于降低生产成本。在过去化肥生产企业用电享有优惠电价，而该优惠政策将于2016年6月前全部取消，这将给企业带来严峻考验。然而大型气化炉如鲁奇炉、德士古、壳牌、航天炉、清华炉、科林炉等的气化压力均在4.0MPa以上，而固定床常压间歇炉的压力又不超过0.01MPa。若能使气化炉生产出的水煤气压力维持在1.0～2.2MPa范围，不仅能满足CO变化压力需要，大幅降低电耗，同时其他物资消耗也会随之降低。并且，冶金、陶瓷、造纸、建材等企业对1.0～2.2MPa中间档压力水煤气也有生产上的需求，这些企业过去多采用天然气，生产成本较高，而等热值情况下水煤气的成本仅是天然气成本的1/2左右。In order to adjust the gas composition, small and medium-sized chemical fertilizer production enterprises are equipped with a carbon monoxide conversion process. There are mainly two types of conversion pressure: 0.8-1.0MPa and 2.0-2.2MPa. Only pressure can be used, so a large amount of electric energy is consumed, and electricity consumption accounts for nearly 30% of the cost of synthetic ammonia, which is not conducive to reducing production costs. In the past, chemical fertilizer production enterprises enjoyed preferential electricity prices, and this preferential policy will be canceled before June 2016, which will bring severe tests to enterprises. However, the gasification pressure of large-scale gasification furnaces such as Lurgi furnace, Texaco, Shell, Aerospace furnace, Tsinghua furnace, Kelin furnace, etc. are all above 4.0MPa, while the pressure of fixed bed atmospheric batch furnace is not more than 0.01MPa . If the pressure of the water gas produced by the gasifier can be maintained in the range of 1.0-2.2MPa, it will not only meet the pressure change requirements of CO, greatly reduce the power consumption, but also reduce the consumption of other materials. Moreover, metallurgy, ceramics, papermaking, building materials and other enterprises also have production demands for water gas with intermediate pressure of 1.0-2.2MPa. About 1/2 of the cost.
公开号CN104673390A的发明专利公开了一种高温焦炭直接气化工艺，包括：1)用未经熄焦的高温焦炭由焦炉推焦进入高温焦罐，通过牵引车送至提升井由提升机提升至气化炉顶；2)高温焦罐通过自动对位系统和炉顶部的高温储料仓对位同时打开卸料阀门将高温焦炭自动落入储料仓，储料仓同时具备储料、破碎机加料功能，能实现自动定时定量将焦炭加入炉中；3)制气用的氧化剂氧气来自空分工序，氧气浓度根据后工序用气要求在40％～100％范围内任意选择，蒸汽来自锅炉和自产蒸汽，氧气和气化剂进入混合罐中混合，从底部进入造气炉，在炉内高温条件下，与高温焦炭进行氧化还原反应，连续生产水煤气；4)反应生成的水煤气自炉顶排出，经过高温除尘器进行除尘后，进入废热锅炉回收高温气体余热，副产压力0.4～3.9MPa的蒸汽；5)出废热锅炉温度80～160℃的水煤气进入洗气塔底部，在塔中用来自造气污水处理系统的闭路循环冷却水喷淋冷却洗涤，将其冷却到40～45℃并洗涤其中夹带的尘埃后，进入煤气总管去后续工段，塔底排出的造气污水通过地沟排至造气污水处理系统，经处理后的循环冷却水由泵送回造气气化系统闭路循环使用。该方法利用高温焦炭的温度在气化炉内形成整体高温区，利于气化反应的进行，能产生高有效成分的煤气，并降低碳和气化剂的消耗。但是该反应在常压下进行，输出的水煤气需经煤气压缩机压缩后送去后续工段。The invention patent with the publication number CN104673390A discloses a direct gasification process of high-temperature coke, including: 1) using unquenched high-temperature coke to push coke from the coke oven into the high-temperature coke tank, and send it to the lifting shaft by a tractor to be lifted by a hoist to the top of the gasification furnace; 2) The high-temperature coke tank is aligned with the high-temperature storage bin on the top of the furnace through the automatic alignment system and at the same time the discharge valve is opened to automatically drop the high-temperature coke into the storage bin. Machine feeding function, which can realize automatic timing and quantitative feeding of coke into the furnace; 3) The oxidant oxygen used for gas production comes from the air separation process, and the oxygen concentration can be arbitrarily selected within the range of 40% to 100% according to the gas requirements of the subsequent process, and the steam comes from the boiler Mix with self-produced steam, oxygen and gasification agent into the mixing tank, enter the gas-making furnace from the bottom, and perform redox reaction with high-temperature coke under high temperature conditions in the furnace to continuously produce water gas; 4) The water gas generated by the reaction comes from the top of the furnace After being discharged by the high-temperature dust collector for dust removal, it enters the waste heat boiler to recover the waste heat of the high-temperature gas, and steam with a pressure of 0.4-3.9MPa is produced as a by-product; The closed-circuit circulating cooling water from the gas-making sewage treatment system is sprayed, cooled and washed, cooled to 40-45°C and the dust entrained in it is washed, and then enters the gas main pipe to the follow-up section, and the gas-making sewage discharged from the bottom of the tower is discharged through the ditch to In the gas-making sewage treatment system, the treated circulating cooling water is pumped back to the gas-making gasification system for closed-circuit recycling. The method uses the temperature of high-temperature coke to form an overall high-temperature zone in the gasification furnace, which is beneficial to the gasification reaction, can produce high-active-component coal gas, and reduces the consumption of carbon and gasification agent. However, the reaction is carried out under normal pressure, and the output water gas needs to be compressed by a gas compressor and then sent to the follow-up section.
发明内容Contents of the invention
本发明的目的是提供一种固定床气化生产1.0～2.2MPa水煤气的方法，该方法能提高原料煤和/或焦炭的转化率，增大煤气中有效成分含量，所产水煤气无需压缩，可直接送往变换工段，节能降耗效果显著。The purpose of the present invention is to provide a method for producing 1.0-2.2MPa water gas by fixed bed gasification, which can improve the conversion rate of raw coal and/or coke, increase the content of active ingredients in the gas, and produce water gas without compression, which can be Directly sent to the transformation section, the effect of energy saving and consumption reduction is remarkable.
为了实现以上目的，本发明所采用的技术方案是：In order to achieve the above object, the technical solution adopted in the present invention is:
固定床气化生产1.0～2.2MPa水煤气的方法，包括以下步骤：将原料煤和/或焦炭加入气化炉中，同时将压力1.2～2.4MPa、浓度≥99.6％的氧气以及平均温度240～270℃、压力1.2～2.4MPa的蒸汽通入气化炉内，控制气化炉内温度1100～1250℃、压力1.0～2.2MPa，反应生成粗煤气，洗涤、冷却，即得；所述原料煤和/或焦炭的供给量为380～420kg/kNm3煤气，氧气通入量为190～220Nm3/kNm3煤气，蒸汽通入量为600～650kg/kNm3煤气。The method for producing 1.0-2.2 MPa water gas by fixed-bed gasification comprises the following steps: adding raw coal and/or coke into a gasification furnace, and simultaneously injecting oxygen with a pressure of 1.2-2.4 MPa, a concentration ≥ 99.6%, and an average temperature of 240-270 ℃, pressure 1.2-2.4MPa steam into the gasifier, control the temperature in the gasifier 1100-1250℃, pressure 1.0-2.2MPa, react to generate crude gas, washing, cooling, that is; the raw coal and /or the supply rate of coke is 380-420 kg/kNm3 gas, the oxygen feed rate is 190-220 Nm3 /kNm3 gas, and the steam feed rate is 600-650 kg/kNm3 gas.
所述氧气、蒸汽的(入炉)压力高于气化炉内压力0.2MPa左右，以便物料顺利入炉。蒸汽的(入炉)温度高于对应压力下饱和温度40～50℃，以避免冷凝水的产生。The (into the furnace) pressure of the oxygen and steam is about 0.2MPa higher than the internal pressure of the gasification furnace, so that the materials can be smoothly fed into the furnace. The temperature of the steam (into the furnace) is 40-50°C higher than the saturation temperature under the corresponding pressure to avoid the generation of condensed water.
所述气化炉的加料口与加煤锁斗连接，原料煤和/或焦炭由皮带输送至料仓后，加入到加煤锁斗中，对加煤锁斗进行充压处理(充压介质为CO2)，至压力略高于气化炉压力，随后原料煤和/或焦炭由加料口进入炉内与气化剂发生氧化还原反应。加料完毕，对加煤锁斗进行泄压处理，泄压气经除尘后直接排入大气，可替代煤锁气回收系统，进而简化流程、减少投资、提高产气效率，最终实现节能降耗。The charging port of the gasifier is connected to the coaling lock hopper, and after the raw coal and/or coke are transported to the silo by the belt, they are added to the coaling lock hopper, and the coaling lock hopper is pressurized (pressurized medium CO2 ), until the pressure is slightly higher than the pressure of the gasifier, and then the raw coal and/or coke enters the furnace through the feeding port to undergo oxidation-reduction reaction with the gasification agent. After feeding, the coal lock hopper is depressurized, and the depressurized gas is directly discharged into the atmosphere after dust removal, which can replace the coal lock gas recovery system, thereby simplifying the process, reducing investment, improving gas production efficiency, and finally realizing energy saving and consumption reduction.
所述氧气、蒸汽可以以混合气的形式通入。其中氧气来自空分工段，加压(至1.5～2.7MPa、80℃)后经调节阀调节流量(1.2～2.4MPa、80℃)，再进入氧气/蒸汽混合器中。蒸汽由外源蒸汽和内源蒸汽两部分组成，外源蒸汽来自工厂供气官网或者为气化系统独立配置的锅炉，如来自锅炉供气管网的过热蒸汽(1.8～3.0MPa、320～350℃，即中压过热蒸汽)。内源蒸汽即冷却用水与气化炉炉壁发生热交换后副产的内源蒸汽(如换热汽包副产的饱和蒸汽，1.1～2.3MPa、184～219℃)。所述氧气先与外源蒸汽混合，混合后的气体再与内源蒸汽混合通入气化炉内，与炉内的原料煤和/或焦炭发生氧化还原反应。具体的，氧气与外源蒸汽先在氧气/蒸汽混合器中混合，混合后的气体经阻火器后与内源蒸汽混合。The oxygen and steam can be introduced in the form of mixed gas. The oxygen comes from the air separation section, pressurizes (to 1.5-2.7MPa, 80°C), and then adjusts the flow rate (1.2-2.4MPa, 80°C) through the regulating valve, and then enters the oxygen/steam mixer. The steam is composed of external source steam and internal source steam. The external source steam comes from the gas supply equipment of the factory or the boiler independently configured for the gasification system, such as superheated steam from the boiler gas supply pipe network (1.8~3.0MPa, 320~350 ℃, that is, medium pressure superheated steam). Endogenous steam refers to endogenous steam by-produced after heat exchange between cooling water and gasifier wall (such as saturated steam by-produced by heat exchange drum, 1.1-2.3MPa, 184-219℃). The oxygen is first mixed with external steam, and the mixed gas is then mixed with internal steam and passed into the gasification furnace to undergo redox reaction with raw coal and/or coke in the furnace. Specifically, oxygen and external steam are first mixed in an oxygen/steam mixer, and the mixed gas is mixed with internal steam after passing through a flame arrester.
气化炉内主要化学反应式见式1)～5)：The main chemical reaction formulas in the gasifier are shown in formulas 1) to 5):
1)C+O2＝CO2+Q；1) C+O2 =CO2 +Q;
2)2C+O2＝2CO+Q；2) 2C+O2 =2CO+Q;
3)C+CO2＝2CO-Q；3) C+CO2 =2CO-Q;
4)C+2H2O(g)＝CO2+2H2-Q；4) C+2H2 O(g)=CO2 +2H2 -Q;
5)C+H2O(g)＝CO+H2-Q。5) C+H2 O(g)=CO+H2 -Q.
所述气化炉包括炉体以及设于炉体外侧用以实现炉体热交换的换热结构，所述换热结构与换热汽包相连通，冷却用水与气化炉炉壁发生热交换后，再在换热汽包中进行汽水分离，副产所述内源蒸汽。换热汽包主要为气化炉提供冷却用水，同时副产中压蒸汽。气化炉的换热结构包括设于筒体外侧的筒体换热结构以及设于气化炉锥底外侧的锥底换热结构。所述氧化还原反应进行时，从管网来的锅炉给水(1.8～3.0MPa、104℃，即脱盐除氧水)通过管道进入气化炉锥底换热结构中，一方面降低炉底温度，防止灰渣温度过高导致炉底超温，影响设备强度，另一方面对锅炉水进行预热(至温度约112.5℃)。预热后的锅炉水进入换热汽包补水，补水后的汽包水再进入气化炉筒体换热结构进行热交换，吸收气化炉炉壁的部分热量后返回换热汽包，在换热汽包中进行汽水分离，并副产内源蒸汽(1.1～2.3MPa、184～219℃，即饱和蒸汽)。The gasification furnace includes a furnace body and a heat exchange structure arranged outside the furnace body to realize heat exchange of the furnace body. The heat exchange structure communicates with the heat exchange drum, and the cooling water exchanges heat with the wall of the gasification furnace. Afterwards, steam-water separation is carried out in the heat exchange steam drum, and the internal source steam is produced as a by-product. The heat exchange drum mainly provides cooling water for the gasifier and produces medium-pressure steam by-product. The heat exchange structure of the gasifier includes a cylinder heat exchange structure arranged outside the cylinder body and a cone bottom heat exchange structure arranged outside the cone bottom of the gasifier. When the oxidation-reduction reaction is in progress, the boiler feed water (1.8-3.0MPa, 104°C, namely desalted and deoxygenated water) from the pipe network enters the conical bottom heat exchange structure of the gasifier through the pipes. On the one hand, the furnace bottom temperature is lowered, To prevent the overheating of the bottom of the furnace caused by the high temperature of ash and slag, which will affect the strength of the equipment, on the other hand, preheat the boiler water (to a temperature of about 112.5°C). The preheated boiler water enters the heat exchange drum for water replenishment, and then the replenished steam drum water enters the heat exchange structure of the gasifier shell for heat exchange, and returns to the heat exchange drum after absorbing part of the heat from the gasifier wall. Steam-water separation is carried out in the heat exchange steam drum, and endogenous steam (1.1-2.3MPa, 184-219°C, namely saturated steam) is produced by-product.
所述气化炉的出气口与文丘里洗涤器连接，气化反应产生的粗煤气(1.0～2.2MPa、温度450～500℃)从出气口出来后，进入文丘里洗涤器中进行增湿、洗涤和冷却处理。洗涤器内洗涤用水由造气循环水管网提供，经增压处理后进入文丘里洗涤器(温度≤45℃)。文丘里洗涤器与煤气洗涤分离器连接，从文丘里洗涤器出来的水煤气(温度约250℃)进入煤气洗涤分离器中进行气水分离。煤气洗涤分离器的顶部设有喷淋装置和填料层，水煤气进入煤气洗涤分离器中，经二次洗涤和冷却处理后(温度降至200℃)送出界区。分离器内喷淋用水同样由造气循环水管网提供，经洗涤、冷却后的水(温度约85℃)从煤气洗涤分离器的底部排入地沟，去往造气循环水处理系统，经沉降、冷却等措施处理后，再进入造气循环水管网中，经造气循环水泵送入文丘里洗涤器和煤气洗涤分离器内循环使用。The gas outlet of the gasification furnace is connected to the Venturi scrubber, and the crude gas (1.0-2.2MPa, temperature 450-500°C) produced by the gasification reaction comes out of the gas outlet and enters the Venturi scrubber for humidification, Wash and cool down. The washing water in the scrubber is provided by the gas-generating circulating water pipe network, and enters the Venturi scrubber (temperature ≤ 45°C) after pressurization treatment. The Venturi scrubber is connected to the gas scrubber separator, and the water gas (temperature about 250°C) from the Venturi scrubber enters the gas scrubber separator for gas-water separation. The top of the gas scrubber is equipped with a spray device and a packing layer. The water gas enters the gas scrubber and is sent out of the boundary area after secondary washing and cooling (temperature drops to 200°C). The water for spraying in the separator is also provided by the gas-generating circulating water pipe network. The washed and cooled water (temperature about 85°C) is discharged from the bottom of the gas-washing separator into the ditch, and goes to the gas-generating circulating water treatment system. After treatment by measures such as cooling and cooling, it enters the gas-making circulating water pipe network, and is sent to the Venturi scrubber and gas scrubber for recycling through the gas-making circulating water pump.
所述气化炉的出灰口与灰锁斗连接，气化反应产生的灰渣经炉篦子破碎、旋刮后进入灰锁斗中，对灰锁斗进行蒸汽充压和加水泄压处理，利用充压、泄压操作实现对灰锁斗的排灰处理。处理后的废水去往造气循环水处理系统，废气经除尘后可直接排入大气。充压蒸汽(1.8～3.0MPa、320～350℃，即中压过热蒸汽)来自锅炉供气管网，泄压用水来自造气循环水管网。The ash outlet of the gasification furnace is connected to the ash lock hopper, and the ash slag produced by the gasification reaction enters the ash lock hopper after being broken by the furnace grate and scraped, and the ash lock hopper is steam-charged and water-added to release the pressure. The ash discharge treatment of the ash lock bucket is realized by the operation of pressure filling and pressure relief. The treated wastewater goes to the gas-making circulating water treatment system, and the waste gas can be directly discharged into the atmosphere after dust removal. The pressurized steam (1.8-3.0MPa, 320-350°C, that is, medium-pressure superheated steam) comes from the boiler gas supply pipe network, and the pressure relief water comes from the gas-making circulating water pipe network.
本发明的有益效果：Beneficial effects of the present invention:
在本发明中，气化炉采用蒸汽升温-氧气点火开车技术，改进了鲁奇炉蒸汽升温-空气点火-氧气开车技术，能简化开车程序和相关工艺流程，减少空气开车设备管道及投资，缩短开车时间，降低开工排放气对环境的污染，增加开车操作的安全性。并且，反应副产中压饱和蒸汽经高位汽包并入中压蒸汽管网，与外来过热蒸汽混合用作气化炉气化剂，可减少新鲜中压蒸汽消耗量。同时，气化系统产生的灰水循环使用，可简化流程，出工段煤气含水饱和度高，下游变换工段无需再添加蒸汽或可少加蒸汽，投资少、耗能低。由于煤气灰水循环利用，其中大部分水溶性气体如氨(NH3)、氢氰酸(HCN)、硫化氢(H2S)等被粗煤气汽提带出，使灰水所含有害气体大为减少。并且，气化后的灰渣采用水力排渣法冲灰，工作量小，操作环境整洁，且便于操作维修，优于其他排渣法。In the present invention, the gasifier adopts the steam heating-oxygen ignition start-up technology, which improves the Lurgi furnace steam heating-air ignition-oxygen start-up technology, which can simplify the start-up procedure and related technological processes, reduce air start-up equipment pipelines and investment, and shorten Reduce the driving time, reduce the environmental pollution caused by the exhaust gas from the start-up, and increase the safety of the driving operation. Moreover, the reaction by-product medium-pressure saturated steam is incorporated into the medium-pressure steam pipe network through the high-level steam drum, and mixed with external superheated steam as the gasification agent of the gasifier, which can reduce the consumption of fresh medium-pressure steam. At the same time, the gray water generated by the gasification system can be recycled, which can simplify the process. The water saturation of the gas in the output section is high, and the downstream transformation section does not need to add steam or can add less steam, with less investment and low energy consumption. Due to the recycling of gas gray water, most of the water-soluble gases such as ammonia (NH3 ), hydrocyanic acid (HCN), hydrogen sulfide (H2 S) and so on are taken out by the stripping of crude gas, so that the harmful gas contained in gray water is greatly increased. for reduction. Moreover, the ash after gasification is washed by hydraulic slag discharge method, which has a small workload, clean operation environment, and is easy to operate and maintain, which is superior to other slag discharge methods.
本发明固定床气化生产1.0～2.2MPa水煤气的方法具有以下优点：1)对煤种的适应反应广，可烧无烟小块煤、褐煤、烟煤、冶金焦、化工焦、兰炭、半焦，也可烧由粉煤制成的煤棒或煤球；2)煤燃烧彻底，炭转化率高，单位煤耗低，在灰熔点以下操作气化，单位氧耗低，相对间歇炉、德士古水煤浆炉、壳牌粉煤炉的蒸汽分解率高；3)现场干净卫生，无噪声、无废水和废气排放，炉渣可用于制作水泥或空心砖，无环保问题，符合国家产业政策；4)煤气有效成分(包括CO、H2和CH4)含量高，煤气热值高；5)水煤气进变换工段前温度高、水汽含量高，变换能耗低，且无需进行变压处理，节能降耗效果显著，吨氨电耗下降400kWh以上。The method for producing 1.0-2.2 MPa water gas by fixed bed gasification of the present invention has the following advantages: 1) It has a wide adaptability to coal types, and can burn anthracite small coal, lignite, bituminous coal, metallurgical coke, chemical coke, semi-coke, semi-coke, etc. Coke, or coal sticks or briquettes made of pulverized coal can also be burned; 2) Coal combustion is complete, the conversion rate of charcoal is high, and the unit coal consumption is low. The gasification is operated below the ash melting point, and the unit oxygen consumption is low. Compared with batch furnaces and taxis Ancient coal-water slurry furnaces and Shell pulverized coal furnaces have a high steam decomposition rate; 3) The site is clean and hygienic, with no noise, no waste water and waste gas emissions, and the slag can be used to make cement or hollow bricks, without environmental protection problems, in line with national industrial policies; 4) Coal gas has high content of effective components (including CO, H2 and CH4 ), and high calorific value of gas; 5) Water gas has high temperature and high water vapor content before entering the transformation section, and low energy consumption for transformation, and no need for pressure transformation treatment, saving energy and reducing consumption The effect is remarkable, and the power consumption per ton of ammonia is reduced by more than 400kWh.
附图说明Description of drawings
图1为实施例中水煤气生产系统的结构示意图；Fig. 1 is the structural representation of water gas production system in the embodiment;
图2为实施例中水煤气生产工艺流程示意图。Fig. 2 is a schematic diagram of the production process of water gas in the embodiment.
具体实施方式detailed description
下述实施例仅对本发明作进一步详细说明，但不构成对本发明的任何限制。The following examples only illustrate the present invention in further detail, but do not constitute any limitation to the present invention.
实施例1Example 1
固定床纯氧连续气化生产2.0MPa水煤气的方法，包括以下步骤：The method for producing 2.0MPa water gas by continuous gasification of pure oxygen in a fixed bed comprises the following steps:
将无烟小块煤(分析指标见下表1)(383kg/kNm3煤气)加入气化炉中，同时将压力2.2MPa的氧气(202Nm3/kNm3煤气)以及温度350℃、压力2.2MPa的外源蒸汽(330kg/kNm3煤气)和温度215℃、压力2.1MPa的内源蒸汽通入气化炉内(蒸汽通入总量为633kg/kNm3煤气)，控制气化炉内温度1100～1200℃、压力2.0MPa(炉顶部测压)，反应生成温度470℃左右的粗煤气，粗煤气经洗涤、冷却，即得温度200℃较洁净的水煤气。Add anthracite small lump coal (see Table 1 below for analysis indicators) (383kg/kNm3 gas) into the gasifier, and at the same time add oxygen at a pressure of 2.2MPa (202Nm3 /kNm3 gas) and a temperature of 350°C and a pressure of 2.2MPa The external source steam (330kg/kNm3 gas) and the internal source steam with a temperature of 215℃ and a pressure of 2.1MPa are passed into the gasifier (the total amount of steam introduced is 633kg/kNm3 gas), and the temperature inside the gasifier is controlled at 1100 ~1200°C, pressure 2.0MPa (pressure measurement at the top of the furnace), the reaction produces crude gas with a temperature of about 470°C, and the crude gas is washed and cooled to obtain clean water gas with a temperature of 200°C.
如图1所示，本实施例中水煤气生产系统包括气化炉7，气化炉7的加料口与加煤锁斗6连接，出灰口与灰锁斗8连接。加料时，无烟小块煤先由皮带输送至料仓，再加入到加煤锁斗6中，利用CO2(由CO2储罐15供给)或中压过热蒸汽对加煤锁斗6进行充压处理，保持压力为2.1MPa，略高于气化炉7内压力(炉内压力2.0MPa)。随后无烟小块煤由加料口进入炉内，与气化剂发生氧化还原反应。加料完毕，对加煤锁斗6进行泄压处理，泄压气经除尘后直接排入大气。As shown in FIG. 1 , the water gas production system in this embodiment includes a gasifier 7 , the feed port of the gasifier 7 is connected to the coal feeding lock hopper 6 , and the ash outlet is connected to the ash lock hopper 8 . When feeding, the anthracite small lump coal is first conveyed to the hopper by the belt, and then added to the coaling lock hopper 6, and the coaling lock hopper 6 is heated by CO2 (supplied by the CO2 storage tank 15) or medium-pressure superheated steam. Pressurization treatment, keep the pressure at 2.1MPa, which is slightly higher than the pressure in the gasification furnace 7 (the pressure in the furnace is 2.0MPa). Then the small pieces of anthracite coal enter the furnace through the feeding port and undergo redox reactions with the gasification agent. After the feeding is completed, the coaling lock hopper 6 is subjected to pressure relief treatment, and the pressure relief gas is directly discharged into the atmosphere after being dedusted.
所述气化剂即为氧气和蒸汽，在本实施例中，氧气来自空分工段1，先经氧压机加压至2.5MPa、80℃送入气化界区，再经调节阀调节流量后(2.2MPa、80℃)进入氧气/蒸汽混合器4中。蒸汽一部分蒸汽来自锅炉供气管网2，为中压过热蒸汽(3.0MPa、350℃)，经调节阀减压至2.2MPa后进入氧气/蒸汽混合器4中。这两路气在氧气/蒸汽混合器中混合，混合后的气体经阻火器并入炉底进气总管，与换热汽包9中副产的中压蒸汽(也即内源蒸汽，2.1MPa、215℃)一同进入气化炉7中，与炉内的无烟小块煤发生氧化还原反应。图1中，另有一路中压蒸汽经环形管直接进入气化炉内，此路蒸汽也作为气化剂使用，当出现严重超温时用以快速调节气化层的温度，但相对用量较少，也不经常用，可不作计算。The gasification agent is oxygen and steam. In this embodiment, the oxygen comes from the air separation section 1. It is first pressurized to 2.5 MPa and sent to the gasification boundary area at 80°C by an oxygen compressor, and then the flow rate is adjusted by a regulating valve. Then (2.2MPa, 80°C) enters the oxygen/steam mixer 4. Steam Part of the steam comes from the boiler gas supply pipe network 2, which is medium-pressure superheated steam (3.0MPa, 350°C), which is decompressed to 2.2MPa by the regulating valve and then enters the oxygen/steam mixer 4. These two paths of gas are mixed in the oxygen/steam mixer, and the mixed gas is merged into the furnace bottom inlet main pipe through the flame arrester, and the medium-pressure steam (that is, internal source steam, 2.1MPa) by-produced in the heat exchange drum 9 , 215°C) into the gasification furnace 7 together, and redox reaction occurs with the anthracite small lump coal in the furnace. In Fig. 1, there is another path of medium-pressure steam directly entering the gasification furnace through the annular pipe. This path of steam is also used as a gasification agent to quickly adjust the temperature of the gasification layer when serious overtemperature occurs, but the relative amount is relatively small. Less, not often used, do not count.
所述气化炉7包括炉体以及设于炉体外侧用以实现炉体热交换的换热结构，换热结构与换热汽包9相连通，换热汽包9主要为气化炉提供冷却水，同时副产内源蒸汽。气化炉的换热结构包括设于气化炉筒体外侧的筒体换热结构以及设于气化炉锥底外侧的锥底换热结构，炉内气化反应进行时，从锅炉供水管网3来的脱盐除氧水(3.0MPa、104℃)经调节阀先进入气化炉锥底换热结构中，一方面降低炉底温度，防止灰渣温度过高导致炉底超温，影响设备强度，另一方面对锅炉水进行预热，至温度约112.5℃，预热后的锅炉水进入换热汽包9中补水，补水后的汽包水再进入气化炉筒体换热结构中进行冷却换热，吸收气化炉炉壁的部分热量后形成饱和水，返回换热汽包9中进行汽水分离，副产压力2.1MPa、温度215℃的中压饱和蒸汽。炉内产生的灰渣由出灰口排出，经炉箅子破碎、旋刮后进入灰锁斗8中。对灰锁斗8进行蒸汽充压和加水泄压处理，利用充压、泄压操作实现对灰锁斗8的排灰处理。其中充压蒸汽为中压过热蒸汽，来自锅炉供气管网2，泄压用水来自造气循环水管网12，处理后的废水去往造气循环水处理系统13，废气经除尘后直接排入大气。The gasification furnace 7 includes a furnace body and a heat exchange structure arranged on the outside of the furnace body to realize the heat exchange of the furnace body. The heat exchange structure is connected with the heat exchange drum 9, and the heat exchange drum 9 mainly provides the gasifier. Cooling water while by-producing endogenous steam. The heat exchange structure of the gasifier includes the cylinder heat exchange structure located outside the gasifier cylinder and the cone bottom heat exchange structure located outside the gasifier cone bottom. When the gasification reaction in the furnace is in progress, the boiler water supply pipe The desalted and deoxygenated water (3.0MPa, 104°C) from network 3 first enters the conical bottom heat exchange structure of the gasifier through the regulating valve. On the other hand, the boiler water is preheated to a temperature of about 112.5°C. The preheated boiler water enters the heat exchange drum 9 to make up water, and the water in the steam drum after water replenishment enters the heat exchange structure of the gasifier cylinder Cooling and heat exchange in the gasification furnace, absorbing part of the heat of the gasification furnace wall to form saturated water, returning to the heat exchange drum 9 for steam-water separation, and producing medium-pressure saturated steam with a pressure of 2.1MPa and a temperature of 215°C. The ash generated in the furnace is discharged from the ash outlet, and enters the ash lock hopper 8 after being crushed by the furnace grate and scraped by rotation. The ash lock hopper 8 is subjected to steam pressurization and water addition to release the pressure, and the ash discharge treatment of the ash lock hopper 8 is realized by using the pressurization and pressure release operations. Among them, the pressurized steam is medium-pressure superheated steam, which comes from the boiler gas supply pipe network 2, the pressure relief water comes from the gas-making circulating water pipe network 12, and the treated waste water goes to the gas-making circulating water treatment system 13, and the waste gas is directly discharged into the gas-making circulating water treatment system after dust removal. atmosphere.
所述气化炉7的出气口与文丘里洗涤器10连接，炉内气化反应产生的粗煤气(2.0MPa、温度470℃左右)从气化炉7的出气口出来后，进入文丘里洗涤器10中增湿、洗涤和冷却。文丘里洗涤器10内的洗涤用水由造气循环水管网12提供，来水经增压处理后进入洗涤器中(温度≤45℃)。The gas outlet of the gasifier 7 is connected to the Venturi scrubber 10, and the crude gas (2.0 MPa, temperature about 470° C.) produced by the gasification reaction in the furnace comes out of the gas outlet of the gasifier 7 and enters the Venturi scrubber. Humidification, washing and cooling in the container 10. The washing water in the Venturi scrubber 10 is provided by the gas-generating circulating water pipe network 12, and the incoming water enters the scrubber after being pressurized (temperature ≤ 45° C.).
所述文丘里洗涤器10还与煤气洗涤分离器11连接，从洗涤器出来的水煤气(温度约250℃)进入煤气洗涤分离器11内进行气水分离。煤气洗涤分离器11的顶部设有喷淋装置和填料层，经洗涤器洗涤、冷却的水煤气进入分离器中，经二次洗涤和冷却处理后降温至200℃，送出界区进入下个工段16。分离器内喷淋用水同样由造气循环水管网12提供，经洗涤、冷却后的水(温度约85℃)从煤气洗涤分离器11的底部排入地沟，去往造气循环水处理系统12，经沉降、冷却等措施处理后，再进入造气循环水管网中，经造气循环水泵14送入文丘里洗涤器10和煤气洗涤分离器11中循环使用。The Venturi scrubber 10 is also connected to the gas scrubber 11, and the water gas (temperature about 250° C.) coming out of the scrubber enters the gas scrubber 11 for gas-water separation. The top of the gas washing separator 11 is equipped with a spraying device and a packing layer. The water gas washed and cooled by the scrubber enters the separator, and after the secondary washing and cooling treatment, the temperature is lowered to 200°C, and it is sent out of the boundary area and enters the next section 16 . The water for spraying in the separator is also provided by the gas-generating circulating water pipe network 12, and the washed and cooled water (temperature about 85°C) is discharged from the bottom of the gas-washing separator 11 into the trench, and goes to the gas-generating circulating water treatment system 12 , after settling, cooling and other measures, it enters the gas-making circulating water pipe network, and is sent to the Venturi scrubber 10 and the gas washing separator 11 for recycling through the gas-making circulating water pump 14.
本实施例生产的水煤气成分见下表2，气化反应消耗指标见下表3，工艺流程图见图2。炉子带出物少(≤0.2kg/KNm3水煤气)，灰渣残炭低(≤3％)。The composition of the water gas produced in this embodiment is shown in Table 2 below, the gasification reaction consumption index is shown in Table 3 below, and the process flow chart is shown in Figure 2. There are few substances carried out by the furnace (≤0.2kg/KNm3 water gas), and low ash residue carbon (≤3%).
表1无烟小块煤的分析指标(均值)Table 1 Analysis index (mean value) of anthracite small lump coal
表2烧无烟小块煤的水煤气成分(均值)Table 2 Composition of water gas in burning anthracite small lump coal (mean value)
表3气化反应消耗指标(均值)Table 3 Gasification reaction consumption index (mean value)
实施例2Example 2
固定床纯氧连续气化生产2.0MPa水煤气的方法，包括以下步骤：The method for producing 2.0MPa water gas by continuous gasification of pure oxygen in a fixed bed comprises the following steps:
将小粒焦炭(分析指标见下表4)(411kg/kNm3煤气)加入气化炉中，同时将压力2.2MPa的氧气(219Nm3/kNm3煤气)以及温度350℃、压力2.2MPa的外源蒸汽(302kg/kNm3煤气)和温度215℃、压力2.1MPa的内源蒸汽通入气化炉内(蒸汽通入总量为602kg/kNm3煤气)，控制气化炉内温度1100～1200℃、压力2.0MPa(炉顶部测压)，反应生成温度480℃左右的粗煤气，粗煤气经洗涤、冷却，即得温度200℃较洁净的水煤气。水煤气生产系统同实施例1，水煤气成分见下表5，气化反应消耗指标见下表6。炉子带出物少(≤0.2kg/KNm3水煤气)，灰渣残炭低(≤3％)。Add small coke (see Table 4 below for the analysis index) (411kg/kNm3 gas) into the gasifier, and at the same time, oxygen at a pressure of 2.2MPa (219Nm3 /kNm3 gas) and an external source at a temperature of 350°C and a pressure of 2.2MPa Steam (302kg/kNm3 gas) and internal source steam with a temperature of 215°C and a pressure of 2.1MPa are passed into the gasifier (the total amount of steam introduced is 602kg/kNm3 gas), and the temperature inside the gasifier is controlled at 1100-1200°C , pressure 2.0MPa (pressure measurement at the top of the furnace), the reaction generates crude gas with a temperature of about 480°C, and the crude gas is washed and cooled to obtain clean water gas with a temperature of 200°C. The water gas production system is the same as in Example 1, the water gas composition is shown in Table 5 below, and the gasification reaction consumption index is shown in Table 6 below. There are few substances carried out by the furnace (≤0.2kg/KNm3 water gas), and low ash residue carbon (≤3%).
表4小粒焦炭的分析指标(均值)Table 4 Analysis index (mean value) of small particle coke
表5烧小粒焦炭的水煤气成分(均值)Table 5 Water gas composition (mean value) of burning small particle coke
表6气化反应消耗指标(均值)Table 6 Gasification reaction consumption index (mean value)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111396460.7ACN114015473A (en) | 2016-05-30 | 2016-05-30 | Method and device for pressurized production of 1.0~2.2MPa water gas with pure oxygen |
| CN201610371210.0ACN105802672A (en) | 2016-05-30 | 2016-05-30 | Method for producing 1.0~2.2MPa water gas by fixed bed gasification |
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610371210.0ACN105802672A (en) | 2016-05-30 | 2016-05-30 | Method for producing 1.0~2.2MPa water gas by fixed bed gasification |
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111396460.7ADivisionCN114015473A (en) | 2016-05-30 | 2016-05-30 | Method and device for pressurized production of 1.0~2.2MPa water gas with pure oxygen |
| Publication Number | Publication Date |
|---|---|
| CN105802672Atrue CN105802672A (en) | 2016-07-27 |
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111396460.7APendingCN114015473A (en) | 2016-05-30 | 2016-05-30 | Method and device for pressurized production of 1.0~2.2MPa water gas with pure oxygen |
| CN201610371210.0APendingCN105802672A (en) | 2016-05-30 | 2016-05-30 | Method for producing 1.0~2.2MPa water gas by fixed bed gasification |
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111396460.7APendingCN114015473A (en) | 2016-05-30 | 2016-05-30 | Method and device for pressurized production of 1.0~2.2MPa water gas with pure oxygen |
| Country | Link |
|---|---|
| CN (2) | CN114015473A (en) |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107446626A (en)* | 2017-08-08 | 2017-12-08 | 北京众联盛化工工程有限公司 | A kind of coke pressurization continuous gasification production method |
| CN108913216A (en)* | 2018-08-06 | 2018-11-30 | 唐山科源环保技术装备有限公司 | The method for controlling the self-produced vapor superpressure discharge of gas generator |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114410352A (en)* | 2022-02-24 | 2022-04-29 | 安徽科达洁能股份有限公司 | Adjustable waste heat recovery device and method |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3206953A1 (en)* | 1982-02-26 | 1983-09-08 | Veb Gaskombinat Schwarze Pumpe, Ddr 7610 Schwarze Pumpe | A process for the fixed-bed pressure gasification of lignite |
| CN101392187A (en)* | 2008-10-29 | 2009-03-25 | 江西昌昱实业有限公司 | Bidirectional oxygen-enriched continuous etherealization process for atmospheric fixed bed gas furnace |
| CN102559266A (en)* | 2011-12-28 | 2012-07-11 | 河南昌昱实业有限公司 | Method for producing water gas by pure oxygen continuous gasification in fixed bed |
| CN103525465A (en)* | 2013-10-13 | 2014-01-22 | 上海穗杉实业有限公司 | Coal gas production method and device using high-temperature rich oxygen and high temperature steam as gasification agent |
| CN205099627U (en)* | 2015-09-08 | 2016-03-23 | 袁峥嵘 | Fixed bed pressurization continuous gasification system water gas system |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3206953A1 (en)* | 1982-02-26 | 1983-09-08 | Veb Gaskombinat Schwarze Pumpe, Ddr 7610 Schwarze Pumpe | A process for the fixed-bed pressure gasification of lignite |
| CN101392187A (en)* | 2008-10-29 | 2009-03-25 | 江西昌昱实业有限公司 | Bidirectional oxygen-enriched continuous etherealization process for atmospheric fixed bed gas furnace |
| CN102559266A (en)* | 2011-12-28 | 2012-07-11 | 河南昌昱实业有限公司 | Method for producing water gas by pure oxygen continuous gasification in fixed bed |
| CN103525465A (en)* | 2013-10-13 | 2014-01-22 | 上海穗杉实业有限公司 | Coal gas production method and device using high-temperature rich oxygen and high temperature steam as gasification agent |
| CN205099627U (en)* | 2015-09-08 | 2016-03-23 | 袁峥嵘 | Fixed bed pressurization continuous gasification system water gas system |
| Title |
|---|
| 王永刚等: "《煤化工工艺学》", 30 September 2014, 中国矿业大学出版社* |
| 王鹏等: "《煤炭气化》", 31 January 2015, 中国石化出版社* |
| 陈景华等: "《无机非金属材料热工过程及设备》", 30 April 2015, 华东理工大学出版社* |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107446626A (en)* | 2017-08-08 | 2017-12-08 | 北京众联盛化工工程有限公司 | A kind of coke pressurization continuous gasification production method |
| CN108913216A (en)* | 2018-08-06 | 2018-11-30 | 唐山科源环保技术装备有限公司 | The method for controlling the self-produced vapor superpressure discharge of gas generator |
| Publication number | Publication date |
|---|---|
| CN114015473A (en) | 2022-02-08 |
| Publication | Publication Date | Title |
|---|---|---|
| CN102533345B (en) | Combined fluidized bed coal gasification method and device | |
| AU2015237094B2 (en) | Solid fuel staged gasification-combustion dual-bed polygeneration system and method | |
| CN106554826B (en) | Circulating fluidized bed coal gasification method and device with fine ash fusion | |
| CN202610195U (en) | Device for preparing ammonia synthesis gas through pressurization and continuous gasification of anthracite | |
| CN104593083A (en) | Novel biomass step-by-step gasification method and device | |
| CN114686633A (en) | Method for pre-heat exchanging hydrogen by utilizing direct reduction iron furnace top gas | |
| CN110373230A (en) | A kind of method that fluidized gasification flying dust returns furnace gas | |
| CN115216346A (en) | Method and system for preparing hydrogen-rich gas by using organic solid waste | |
| CN101250419A (en) | A kind of coal gas internal heat low-temperature dry distillation method | |
| CN101760244B (en) | Three-phase multi-raw-material pressurized coal gasification device and process thereof | |
| CN105802672A (en) | Method for producing 1.0~2.2MPa water gas by fixed bed gasification | |
| CN107118807B (en) | System and method for preparing reducing gas by lignite double-bed gasification | |
| CN103435041A (en) | Method and system for producing calcium carbide with biomass fuel | |
| CN105062568B (en) | Method for utilizing coal and natural gas jointly to produce synthesis gas | |
| CN110205165A (en) | A kind of combination cot gasification system and method | |
| CN114317855A (en) | A method of blast furnace ironmaking | |
| CN107987889B (en) | Energy-saving and emission-reducing method for semi-coke gasification gas boiler | |
| CN204417437U (en) | A kind of novel biomass substep gasification installation | |
| CN114737002B (en) | Method for compositely blowing biomass hydrogen-rich micro powder and biomass synthesis gas | |
| CN113969193B (en) | Heat energy recovery gasification metallurgy integrated process | |
| CN216192109U (en) | Coke powder gasification system and pyrolysis gasification integrated system | |
| CN107164594B (en) | System and method for producing direct reduced iron by double reforming and conversion of BGL gasification gas | |
| CN112662436A (en) | Anthracite low-methane gasification process and gasifier | |
| CN111171874B (en) | Process for preparing synthetic gas or fuel gas by moving bed pure oxygen continuous gasification furnace for cow dung raw material | |
| CN104164257A (en) | Fischer-Tropsch reactor pure-oxygen continuous gasification apparatus and gasification technology |
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | Application publication date:20160727 | |
| RJ01 | Rejection of invention patent application after publication |