焦化气发电机组的煤气的初冷和焦油的回收

　　Initial cooling of coal gas and recovery of tar in coking gas generator units

　　荒煤气的主要成分有净焦炉煤气、水蒸气、煤焦油气、苯族烃、氨、萘、硫化氢、其他硫化物、氰化氢等氰化物、吡啶盐等。

　　The main components of raw coal gas include clean coke oven gas, steam, coal coke oil and gas, benzene hydrocarbons, ammonia, naphthalene, hydrogen sulfide, other sulfides, cyanide such as hydrogen cyanide, pyridines, etc.

　　回收炼焦化学产品具有重要的意义。煤在炼焦时，除有75%左右变成焦炭外，还有25%左右生成多种化学产品及煤气。来自焦炉的荒煤气，经冷却和用各种吸收剂处理后，可以提取出煤焦油、氨、萘、硫化氢、氰化氢及粗苯等化学产品，并得到净焦炉煤气，氨可以用于制取硫酸铵和无水氨；煤气中所含的氢可用于制造合成氨、合成甲醇、双氧水、环己烷等，合成氨可进一步制成硫酸铵等化肥；所含的乙烯可用于制取乙醇和三氯乙烷的原料，硫化氢是生产单质硫和元素硫的原料，氰化氢可用于制取黄血盐钠或黄血盐钾；粗苯和煤焦油都是很复杂的半成品，经精制加工后，可得到的产品有：二硫化碳、苯、甲苯、三甲苯、古马隆、酚、甲酚和吡啶盐及沥青等，这些产品有广泛的用途，是合成纤维、塑料、染料、合成橡胶、医药、农药、耐辐射材料、耐高温材料以及国防工业的重要原料。

　　The recycling of coking chemical products is of great significance. During coking, about 75% of coal is converted into coke, and another 25% is used to produce various chemical products and coal gas. The raw gas from coke ovens can be cooled and treated with various absorbents to extract chemical products such as coal tar, ammonia, naphthalene, hydrogen sulfide, hydrogen cyanide, and crude benzene, and obtain clean coke oven gas. Ammonia can be used to produce ammonium sulfate and anhydrous ammonia; The hydrogen contained in coal gas can be used to produce synthetic ammonia, synthetic methanol, hydrogen peroxide, cyclohexane, etc. Synthetic ammonia can be further used to produce fertilizers such as ammonium sulfate; The ethylene contained can be used as a raw material for producing ethanol and trichloroethane, hydrogen sulfide is a raw material for producing elemental sulfur and elemental sulfur, and hydrogen cyanide can be used to produce sodium or potassium yellow blood salt; Crude benzene and coal tar are both complex semi-finished products that can be refined and processed to obtain products such as carbon disulfide, benzene, toluene, trimethylbenzene, coumarin, phenol, cresol, pyridinium salts, and asphalt. These products have a wide range of applications and are important raw materials for synthetic fibers, plastics, dyes, synthetic rubber, pharmaceuticals, pesticides, radiation resistant materials, high-temperature resistant materials, and defense industries.

　　回收工艺的组成为：焦炉炭化室生成的荒煤气在化学产品回收车间进行冷却、输送、回收煤焦油、氨、硫、苯族烃等化学产品，同时净化煤气。化产回收车间一般由冷凝鼓风工段、HPF脱硫工段、硫铵工段、终冷洗苯工段、粗苯蒸馏工段等工段组成。

　　The composition of the recycling process is as follows: the raw coal gas generated in the coking chamber of the coke oven is cooled, transported, and recycled in the chemical product recycling workshop to produce chemical products such as coal tar, ammonia, sulfur, and benzene hydrocarbons, while purifying the gas. The chemical recovery workshop generally consists of condensing and blowing section, HPF desulfurization section, ammonium sulfate section, final cold washing benzene section, crude benzene distillation section and other sections.

　　冷凝工段

　　Condensation section

　　1、煤气的初冷和焦油氨水的分离

　　1. Initial cooling of coal gas and separation of tar and ammonia water

　　2、煤气初冷的目的一是冷却煤气，二是使焦油和氨水分离，并脱除焦油渣。

　　2. The purpose of initial gas cooling is twofold: firstly, to cool the gas; secondly, to separate tar and ammonia water, and to remove tar residue.

　　在炼焦过程中，从焦炉碳化室经上升管逸出的粗煤气温度为650～750℃，首先经过初冷，将煤气温度降至25～35℃，粗煤气中所含的大部分水汽、焦油气、萘及固体微粒被分离出来，部分硫化氢和氰化氢等腐蚀性物质溶于冷凝液中，从而可减少回收设备及管道的堵塞和腐蚀；煤气经初冷后，体积变小，从而使鼓风机以较小的动力消耗将煤气送往后续的净化工序；煤气经出冷后，温度降低，是保证炼焦化学产品回收率和质量的先决条件。

　　During the coking process, the temperature of the crude gas escaping from the carbonization chamber of the coke oven through the riser is 650-750 ℃. Firstly, it is cooled down to 25-35 ℃, and most of the water vapor, tar gas, naphthalene, and solid particles contained in the crude gas are separated. Some corrosive substances such as hydrogen sulfide and cyanide dissolve in the condensate, thereby reducing the blockage and corrosion of recovery equipment and pipelines; After initial cooling, the volume of gas decreases, allowing the blower to send the gas to the subsequent purification process with less power consumption; After the gas is cooled, the temperature decreases, which is a prerequisite for ensuring the recovery rate and quality of coking chemical products.

　　煤气的初冷分为集气管冷却和初冷器冷却两个步骤。

　　The initial cooling of gas is divided into two steps: gas collection pipe cooling and primary cooler cooling.

　　1.1煤气在集气管内的冷却

　　1.1 Cooling of Gas in Gas Collecting Pipeline

　　煤气在集气管内冷却机理

　　Cooling mechanism of gas in the gas collection pipeline

　　煤气在桥管和集气管内的冷却，是用表压为147～196Kpa，温度为70～75℃的循环氨水通过喷头强烈喷洒进行的。当细雾状的氨水与煤气充分接触时，由于煤气温度很高而湿度又很低，故煤气放出大量的显热，氨水大量蒸发，快速进行着传热和传质过程。传热过程取决于煤气与氨水的温度差，所传递的热量为显热，约占煤气冷却所放出总热量的10%～15%。传质过程的推动力是循环氨水液面上的蒸汽分压与煤气中蒸汽分压之差，氨水部分蒸发，煤气温度急剧降低，以供给氨水蒸发所需的潜热，此部分热量约占煤气冷却所放出热量的75%～80%。另有约占所放出总热量10%的热量由集气管表面散失。

　　The cooling of gas in the bridge pipe and gas collection pipe is carried out by vigorously spraying circulating ammonia water with a gauge pressure of 147-196Kpa and a temperature of 70-75 ℃ through a nozzle. When the fine mist like ammonia water comes into full contact with the gas, due to the high temperature and low humidity of the gas, a large amount of sensible heat is released from the gas, and the ammonia water evaporates rapidly, carrying out heat and mass transfer processes. The heat transfer process depends on the temperature difference between gas and ammonia water, and the heat transferred is sensible heat, accounting for about 10% to 15% of the total heat released by gas cooling. The driving force of mass transfer process is the difference between the vapor partial pressure on the circulating ammonia water surface and the vapor partial pressure in the gas. The ammonia water partially evaporates, and the gas temperature drops sharply to supply the latent heat required for ammonia water evaporation. This part of the heat accounts for about 75% to 80% of the heat released by gas cooling. About 10% of the total heat released is dissipated from the surface of the gas collection pipe.

　　通过上述冷却过程，煤气温度由800℃左右降至82～86℃，同时由60%左右的焦油气冷凝下来，这是重质焦油部分。在实际生产过程中，煤气温度可冷却至25℃。（高于其最后达到的露点温度1～3℃）

　　Through the above cooling process, the gas temperature drops from around 800 ℃ to 82-86 ℃, while about 60% of the tar gas is condensed, which is the heavy tar portion. In the actual production process, the gas temperature can be cooled to 25 ℃. (1-3 ℃ higher than its final dew point temperature)

　　1.2 煤气在初冷器内的冷却

　　1.2 Cooling of Gas in the Primary Cooler

　　焦炉煤气由集气管沿吸煤气主管流向煤气初冷器。吸煤气主管除将煤气由焦炉引向化产回收装置外，还起着空气冷却器的作用，煤气可降温1～3℃。

　　Coke oven gas flows from the gas collection pipe along the main gas suction pipe to the gas primary cooler. The main gas suction pipe not only directs the gas from the coke oven to the chemical recovery unit, but also serves as an air cooler, which can cool the gas by 1-3 ℃.

　　煤气进入初冷器的温度仍然很高，达82℃左右，而且含有大量蒸汽和焦油气，须在初冷器中冷却到25～35℃，并将大部分焦油气和蒸汽冷凝下来。

　　The temperature of the gas entering the primary cooler is still very high, reaching around 82 ℃, and it contains a large amount of steam and tar gas. It needs to be cooled to 25-35 ℃ in the primary cooler and most of the tar gas and steam need to be condensed.

　　根据采用的初冷主体设备型式的不同，初冷的方法有间接初冷法、直接初冷法和间接直接初冷法之分。

　　According to the different types of primary cooling equipment used, there are three methods of primary cooling: indirect primary cooling, direct primary cooling, and indirect direct primary cooling.

　　煤气初冷工艺控制的关键操作指标，就是初冷后煤气的出口温度。

　　The key operational indicator for controlling the initial cooling process of gas is the outlet temperature of the gas after initial cooling.

　　（1）煤气中蒸汽含量增多，体积变大，致使鼓风机能力不足，影响煤气正常输送。

　　(1) The increase in steam content and volume in gas leads to insufficient blower capacity, affecting the normal transportation of gas.

　　（2）焦油气凝结率低，初冷后煤气中焦油含量增多，影响以后的工序操作。

　　(2) The low condensation rate of tar gas leads to an increase in tar content in the gas after initial cooling, which affects subsequent process operations.

　　（3）当出口温度高时，煤气中萘含量将更显著增大。这会造成煤气管道和设备堵塞，增加以后洗萘系统负荷，给洗氨、洗苯带来困难。

　　(3) When the outlet temperature is high, the naphthalene content in the gas will increase more significantly. This will cause blockages in gas pipelines and equipment, increase the load on the naphthalene washing system in the future, and pose difficulties for ammonia and benzene washing.

　　因此，在煤气初冷器中，必须保证初冷后集合温度不高于规定值，并尽可能低脱除煤气中的萘。

　　Therefore, in the gas primary cooler, it is necessary to ensure that the collection temperature after initial cooling does not exceed the specified value, and to remove naphthalene from the gas as low as possible.

　　1.3 煤气的初冷流程

　　1.3 Initial cooling process of gas

　　焦油煤气与喷洒氨水、冷凝焦油等沿吸煤气主管首先进入气液分离器，煤气与焦油、氨水、焦油渣等在此分离。分离出来的焦油、氨水和焦油渣一起进入焦油氨水分离槽，经过澄清分成三层：上层为氨水；中层为焦油；下层为焦油渣。沉淀下来的焦油渣由刮板输送机连续刮送至漏斗处排出槽外，有小车定期送往煤场。焦油则通过液面调节器流至氨水中间槽，由此泵往油库工段焦油贮槽。氨水由分离槽上部流至氨水中间槽，再用循环氨水泵送回焦炉集气管以冷却粗煤气，这部分氨水称之为循环氨水。

　　Tar gas, sprayed ammonia water, condensed tar, etc. first enter the gas-liquid separator along the main gas suction pipe, where the gas is separated from tar, ammonia water, tar residue, etc. The separated tar, ammonia water, and tar residue enter the tar ammonia water separation tank together, and after clarification, they are divided into three layers: the upper layer is ammonia water; The middle layer is tar; The lower layer is tar residue. The precipitated tar residue is continuously scraped by a scraper conveyor to the funnel and discharged outside the trough, and is regularly transported to the coal yard by a small car. Tar flows through the liquid level regulator to the ammonia intermediate tank, and is then pumped to the tar storage tank in the oil depot section. Ammonia water flows from the upper part of the separation tank to the intermediate tank, and is then pumped back to the coke oven gas collection pipe by a circulating ammonia water pump to cool the crude gas. This part of ammonia water is called circulating ammonia water.

　　经气液分离后的煤气进入横管式初冷器，横管式初冷器煤气通道，一般上段用循环氨水喷洒，下段用冷凝液喷洒。上段冷凝液从隔断板经水封自流至氨水分离器，下段冷凝液经水封自流至冷凝液槽。下段冷凝液主要是轻质焦油，作为下段喷洒液有利于洗萘。突出特点是横管式初冷器的热负荷显著降低，冷却水用量大为减少。

　　After gas-liquid separation, the coal gas enters the horizontal tube primary cooler. The gas channel of the horizontal tube primary cooler is generally sprayed with circulating ammonia water in the upper section and condensed liquid in the lower section. The upper condensate flows from the partition plate to the ammonia separator through the water seal, while the lower condensate flows to the condensate tank through the water seal. The main component of the lower condensate is light tar, which is beneficial for washing naphthalene as the lower spray liquid. The prominent feature is that the heat load of the horizontal tube primary cooler is significantly reduced, and the amount of cooling water used is greatly reduced.

　　随着煤气的冷却，煤气中剩余的绝大部分的焦油气、蒸汽和萘在初冷器中被冷却下来，萘溶解于焦油中。煤气中一定数量的氨、二氧化碳、硫化氢、氰化氢和其他组分溶解于冷凝水中，形成了冷凝氨水。焦油和冷凝氨水的混合液称为冷凝液。冷凝氨水中含有较多的挥发铵盐，固定铵盐的含量较少。循环氨水中则主要含有固定铵盐，在单独循环使用时，固定铵盐含量可高达30～40g/L。为了降低循环氨水中固定铵盐的含量，以减轻对焦油蒸馏设备的腐蚀和改善焦油的脱水、脱盐操作，大多采用两种氨水混合的流程，混合氨水固定铵盐的含量可降至1.3～3.5 g/L。冷凝液自流入冷凝液槽，再用泵送入机械化刮渣槽，与澄清氨水混合液澄清分离。分离后所得剩余氨水送去脱酚和蒸氨。

　　As the gas cools, the majority of the remaining tar gas, steam, and naphthalene in the gas are cooled down in the primary cooler, and naphthalene dissolves in the tar. A certain amount of ammonia, carbon dioxide, hydrogen sulfide, hydrogen cyanide, and other components in coal gas dissolve in condensate water, forming condensate ammonia water. The mixture of tar and condensed ammonia water is called condensate. Condensed ammonia water contains more volatile ammonium salts and less fixed ammonium salts. The circulating ammonia water mainly contains fixed ammonium salts, and when used separately, the content of fixed ammonium salts can be as high as 30-40 g/L. In order to reduce the content of fixed ammonium salts in circulating ammonia water, alleviate the corrosion of tar distillation equipment, and improve the dehydration and desalination operations of tar, a process of mixing two types of ammonia water is mostly adopted. The content of fixed ammonium salts in mixed ammonia water can be reduced to 1.3-3.5 g/L. The condensate flows into the condensate tank and is then pumped into the mechanized scraper tank for clarification and separation with the clarified ammonia water mixture. The remaining ammonia water obtained after separation is sent for dephenolization and ammonia distillation.

　　由横管式初冷器出来的煤气尚含有1.5～2g/m3的雾状焦油，被鼓风机抽送至电捕焦油器除去绝大部分焦油雾后，送往下一道工序。

　　The gas from the horizontal tube primary cooler still contains 1.5-2g/m3 of misty tar, which is pumped by a blower to an electric tar catcher to remove the majority of tar mist before being sent to the next process.

　　1.4 焦油氨水的分离

　　1.4 Separation of Tar Ammonia Water

　　用循环氨水在集气管内喷洒粗煤气时，约60%的焦油冷凝下来，这种焦油是重质焦油，黏度较大，其中混有一定数量的焦油渣。焦油渣内含有煤尘、焦粉、炭化室顶部热解产生的游离炭及清扫上升管和集气管时所带入的多孔物质，其量约占焦油渣的30%，其余约70%为焦油。焦油渣量一般为焦油质量的0.15%～0.3%。

　　When using circulating ammonia water to spray crude coal gas in the gas collection pipe, about 60% of the tar condenses. This tar is heavy tar with high viscosity and contains a certain amount of tar residue. Tar residue contains coal dust, coke powder, free carbon produced by pyrolysis at the top of the carbonization chamber, and porous substances brought in during the cleaning of the riser and gas collection pipe. Its amount accounts for about 30% of the coke residue, and the remaining 70% is tar. The amount of tar residue is generally 0.15% to 0.3% of the tar mass.

　　焦油渣内固定碳含量约为60%，因其与集气管焦油的密度差小，密度小，易于焦油黏附在一起，所以难分离。

　　The fixed carbon content in tar residue is about 60%, and it is difficult to separate due to its small density difference with the tar in the gas collection pipe, which makes it easy for tar to adhere together.

　　在两种氨水混合分离流程中，初冷器轻质焦油和上述重质焦油混合后，20℃，密度可降至1.15～1.19Kg/L，黏度比重质焦油减少20%～45%，焦油渣易于沉淀下来，混合焦油质量明显改善。但在焦油中仍存在一些浮焦油渣，给焦油分离带来困难。

　　In the two ammonia water mixing and separation processes, after mixing the light tar from the primary cooler with the heavy tar mentioned above, the density can be reduced to 1.15-1.19Kg/L at 20 ℃, and the viscosity can be reduced by 20% -45% compared to the heavy tar. The tar residue is easy to precipitate, and the quality of the mixed tar is significantly improved. However, there are still some floating tar residues in the tar, which pose difficulties for tar separation.

　　经澄清分离后的循环氨水中，焦油物质含量越低越好，最好不超过100mg/L.

　　The lower the tar content in the clarified and separated circulating ammonia water, the better, preferably not exceeding 100mg/L

　　1.5 煤气中焦油雾的清除

　　1.5 Removal of Tar Mist from Gas

　　焦油雾是在煤气冷却过程中形成的，它以内充煤气的焦油气泡状态或极细小的焦油滴存在于煤气中。由于焦油雾又轻又小，其沉降速度小于煤气流速，因而悬浮于煤气中并被煤气带走。

　　Tar mist is formed during the cooling process of coal gas, and it exists in the form of tar bubbles or extremely small tar droplets filled with coal gas. Due to the light and small nature of tar mist, its settling velocity is lower than the gas flow rate, so it is suspended in the gas and carried away by the gas.

　　初冷器后煤气中焦油雾的含量一般为2～5g/m3。鼓风机后煤气中焦油雾的含量一般为0.3～0.5g/m3。化产回收工艺要求煤气中焦油雾的含量低于0.02 g/m3，否则对化产回收操作将有严重影响。

　　The content of tar mist in the gas after the primary cooler is generally 2-5g/m3. The content of tar mist in the gas after the blower is generally 0.3-0.5g/m3. The chemical recovery process requires the tar mist content in the gas to be less than 0.02 g/m3, otherwise it will have a serious impact on the chemical recovery operation.

　　2、冷凝鼓风工段工艺流程：

　　2. Process flow of condensing and blowing section:

　　炼焦过程中产生的荒煤气汇集到炭化室顶部空间，经上升管、桥管进入集气管。约800℃左右的荒煤气在桥管内被循环氨水喷洒冷却到85℃左右。荒煤气中的焦油等同时被冷却下来，焦油和氨水一起沿吸煤气管道至气液分离器，气液分离后荒煤气由上部出来，进入横管初冷器。在此分循环水段、低温水段两段冷却。循环水段用32°C循环水与煤气换热，低温水段用16°C低温水将煤气冷却至25°C。由横管初冷器下部排出的煤气，进入电捕焦油器，除掉煤气中夹带的焦油，经脱硫装置脱硫后，再由鼓风机压送至硫铵装置。

　　The raw gas generated during the coking process is collected in the top space of the carbonization chamber and enters the gas collection pipe through the riser and bridge pipe. The raw gas at around 800 ℃ is cooled to around 85 ℃ by circulating ammonia water spraying inside the bridge pipe. The tar and other substances in the raw gas are simultaneously cooled down, and the tar and ammonia water flow along the gas suction pipeline to the gas-liquid separator. After gas-liquid separation, the raw gas comes out from the upper part and enters the horizontal tube primary cooler. Here, it is divided into two cooling stages: circulating water stage and low-temperature water stage. The circulating water section uses 32 ° C circulating water to exchange heat with the gas, while the low-temperature water section uses 16 ° C low-temperature water to cool the gas to 25 ° C. The gas discharged from the lower part of the horizontal tube primary cooler enters the electric tar catcher to remove the tar carried in the gas. After desulfurization by the desulfurization device, it is then pressurized by the blower to the ammonium sulfate device.

　　为了保证初冷器冷却及除萘效果，在循环水段采用乳化液泵喷洒焦油、氨水的乳化液、在低温水段连续喷洒焦油、氨水混合液，在其顶部用热氨水定期冲洗，以清除管壁上的焦油、萘等杂质。

　　In order to ensure the cooling and naphthalene removal effect of the primary cooler, an emulsion pump is used to spray tar and ammonia emulsion in the circulating water section, and a mixture of tar and ammonia is continuously sprayed in the low-temperature water section. The top is regularly rinsed with hot ammonia water to remove impurities such as tar and naphthalene from the pipe wall.

　　初冷器循环水段的冷凝液排入机械刮渣槽。

　　The condensate from the circulating water section of the primary cooler is discharged into the mechanical scraper tank.

　　初冷器低温水段排出的冷凝液经水封槽流入冷凝液槽，加兑一定量焦油、氨水乳化液后，用泵将其送入初冷器低温水段循环喷洒。

　　The condensate discharged from the low-temperature water section of the primary cooler flows into the condensate tank through the water seal tank. After adding a certain amount of tar and ammonia emulsion, it is pumped into the low-temperature water section of the primary cooler for circulation and spraying.

　　由气液分离器分离下来的焦油、氨水进入机械刮渣槽，在此进行氨水、焦油和焦油渣的分离，氨水和焦油自流入焦油氨水分离槽，焦油渣排入焦油渣小车，定期送往煤场。

　　The tar and ammonia water separated by the gas-liquid separator enter the mechanical scraper tank, where ammonia water, tar, and tar slag are separated. Ammonia water and tar flow into the tar ammonia water separation tank, and the tar slag is discharged into the tar slag trolley and regularly sent to the coal yard.

　　焦油氨水分离槽上部的氨水自流入下部槽内，再由循环氨水泵送至焦炉集气管喷洒冷却煤气，剩余氨水自流入剩余氨水槽，经气浮除焦油器脱除焦油后，送至蒸氨装置处理。焦油氨水分离槽下部的焦油通过溢流瓶自流入焦油中间槽，用焦油泵送油库。焦油氨水分离槽底部的焦油渣用焦油渣泵送机械刮渣槽。

　　The ammonia water from the upper part of the tar ammonia water separation tank flows into the lower tank by itself, and is then pumped by the circulating ammonia water pump to the coke oven gas collection pipe to spray and cool the gas. The remaining ammonia water flows into the remaining ammonia water tank by itself, and after removing tar through the gas flotation tar remover, it is sent to the ammonia distillation unit for treatment. The tar in the lower part of the tar ammonia separation tank flows into the tar intermediate tank through the overflow bottle and is pumped to the oil depot by the tar pump. The tar residue at the bottom of the tar ammonia separation tank is pumped to the mechanical scraping tank using a tar residue pump.

　　3、工艺特点

　　3. Process characteristics

　　1）初冷器采用高效横管冷却器，将煤气冷却到~25°C，使煤气中的大部分萘通过冷却脱除，确保后序设备无堵塞之患。

　　1) The primary cooler adopts an efficient transverse tube cooler to cool the gas to~25 ° C, which removes most of the naphthalene in the gas through cooling and ensures that the subsequent equipment is not blocked.

　　2）横管冷却器中间带断塔盘结构，节约了低温水用量，降低了操作费用。

　　2) The horizontal tube cooler has a broken tray structure in the middle, which saves the amount of low-temperature water and reduces operating costs.

　　3）采用新型高效的蜂窝式电捕焦油器，处理后煤气中焦油可控制在50mg/m3以下，有利于后序设备的正常操作。

　　3) By using a new and efficient honeycomb type electric tar catcher, the tar in the treated gas can be controlled below 50mg/m3, which is beneficial for the normal operation of subsequent equipment.

　　4）采用串联剩余氨水槽静止沉淀和氨水气浮除焦油器除渣除油，降低剩余氨水含油量，有利于蒸氨正常操作。

　　4) The use of a series of residual ammonia water tanks for static precipitation and an ammonia water flotation tar remover for slag and oil removal reduces the oil content of residual ammonia water, which is beneficial for the normal operation of ammonia distillation.

　　5） 高压氨水泵采用变频调速。

　　5) The high-pressure ammonia water pump adopts variable frequency speed regulation.

　　6） 电捕焦油器蜂窝管为不锈钢材质。

　　6) The honeycomb tube of the electric tar catcher is made of stainless steel material.

　　7）煤气鼓风机采用带液力偶合器的高效低耗的电动煤气鼓风机，使煤气鼓风机可根据煤气量实现无级调速，适合焦化厂煤气量周期性波动的特点，并可实现鼓风机前吸煤气管道压力自动调节。同时操作调节灵活，高效节能。

　　7) The gas blower adopts an efficient and low consumption electric gas blower with a hydraulic coupling, which enables the gas blower to achieve stepless speed regulation according to the gas volume, suitable for the periodic fluctuation of gas volume in coking plants, and can automatically adjust the pressure of the gas suction pipeline before the blower. Simultaneously operate and adjust flexibly, efficient and energy-saving.

　　4、主要技术操作指标

　　4. Main technical operation indicators

　　初冷器后煤气温度～25℃

　　Gas temperature after primary cooler~25 ℃

　　初冷器循环水入口温度32℃

　　Initial cooler circulating water inlet temperature 32 ℃

　　初冷器循环水出口温度45℃

　　Initial cooler circulating water outlet temperature 45 ℃

　　初冷器低温水入口温度16℃

　　The inlet temperature of low-temperature water in the primary cooler is 16 ℃

　　初冷器低温水出口温度23℃

　　Low temperature water outlet temperature of primary cooler 23 ℃

　　电捕焦油器绝缘箱温度80～100℃

　　Insulation box temperature of electric tar catcher 80-100 ℃

　　初冷器阻力1.5kPa

　　Initial cooler resistance 1.5kPa

　　电捕焦油器阻力0.5kPa

　　Electric tar catcher resistance 0.5kPa

　　5、主要环保措施

　　5. Main environmental protection measures

　　1）焦油渣回兑炼焦煤中，废渣不外排。

　　1) Tar residue is mixed with coking coal, and the waste residue is not discharged.

　　2）贮槽放散气体经压力平衡系统回吸煤气管道，废气不外排。

　　2) The gas released from the storage tank is sucked back into the gas pipeline through the pressure balance system, and the exhaust gas is not discharged outside.

　　3）设备放空液、泵漏液经地下放空槽送回吸煤气管道，废水不外排。

　　3) The equipment venting liquid and pump leakage liquid are sent back to the gas suction pipeline through the underground venting tank, and the wastewater is not discharged outside.

　　6、主要设备的工作原理

　　6. Working principle of main equipment

　　离心式鼓风机

　　Centrifugal blower

　　离心式鼓风机又称涡轮式鼓风机，由汽轮机或电动机驱动。

　　Centrifugal blower, also known as turbine blower, is driven by a steam turbine or an electric motor.

　　离心式鼓风机由导叶轮、外壳和安装在轴上的工作叶轮所组成。煤气由鼓风机吸入后做高速旋转于转子的第一个工作叶轮中心，煤气在离心力的作用下被甩到壳体的环形空隙中心处即产生减压，煤气就不断的被吸入，离开叶轮时煤气速度很高，当进入环形空隙中，其动压头一部分转变为静压头，煤气的运动速度减小，并通过导管进入第二个叶轮，产生与第一叶轮相同的作用，煤气的静压头再次被提高。从最后一个叶轮出来的煤气由壳体的环形空隙流入出口连接管被送入压出管路中。

　　A centrifugal blower consists of a guide impeller, a casing, and a working impeller installed on the shaft. After being sucked in by the blower, the gas rotates at high speed at the center of the first working impeller of the rotor. Under the action of centrifugal force, the gas is thrown to the center of the annular gap of the shell, which produces pressure reduction. The gas is continuously sucked in and leaves the impeller at a high speed. When it enters the annular gap, a part of its dynamic pressure head is converted into a static pressure head, and the velocity of the gas decreases. It enters the second impeller through the conduit, producing the same effect as the first impeller, and the static pressure head of the gas is increased again. The gas coming out of the last impeller flows into the outlet connecting pipe through the annular gap of the shell and is sent into the extrusion pipeline.

　　煤气输送借助鼓风机将煤气由焦炉吸出，现代使用的鼓风机总压头为30～36KPa，经鼓风机增压后，由于绝热压缩煤气升温10～15℃。煤气鼓风机正常操作是焦化厂生产的关键，它既要输送煤气，又要保持炭化室和集气管的压力稳定，所以必须精心操作和养护。机体下部凝结的焦油和水要及时排出。

　　Gas transportation uses a blower to extract gas from the coke oven. The total pressure head of modern blowers is 30-36KPa. After being pressurized by the blower, the gas is heated by 10-15 ℃ due to adiabatic compression. The normal operation of the gas blower is crucial for the production of coking plants. It not only needs to transport gas, but also maintain stable pressure in the carbonization chamber and gas collection pipe, so it must be carefully operated and maintained. Tar and water condensed in the lower part of the body should be promptly discharged.

　　为什么要在焦化厂煤气流程内设置鼓风机？

　　Why is it necessary to install a blower in the gas process of a coking plant?

　　从炼焦炉出来的焦炉煤气，经集气管、吸气管、初冷器、捕焦油器、回收氨和苯的系统等一系列的设备，然后才能变成净煤气送给不同的用户，或送至贮罐。在这一过程中煤气要克服许多阻力才能达用户的地点，为此煤气应具有足够的剩余压力。另外，为了使焦炉内的荒煤气按规定的压力制度抽出，要使煤气管线中具有一定的吸力。因此，必须在焦化工艺的流程中，选择合理的位置设置鼓风机，使地级前为负压，机后为正压，一般焦化厂鼓风机的位置选择在初冷器之后和电捕焦油器之前，这是因为此时鼓风机的负荷较小，电捕焦油器处于正压状态下操作，比较安全。

　　The coke oven gas from the coke oven can only be converted into clean gas and sent to different users or storage tanks after passing through a series of equipment such as gas collection pipes, suction pipes, primary coolers, tar catchers, and systems for recovering ammonia and benzene. In this process, the gas must overcome many resistance to reach the user's site, so the gas should have sufficient residual pressure. In addition, in order to extract the raw gas from the coke oven according to the prescribed pressure system, it is necessary to provide a certain suction force in the gas pipeline. Therefore, it is necessary to choose a reasonable position to set up the blower in the coking process, so that the ground level front is negative pressure and the rear is positive pressure. Generally, the position of the blower in coking plants is chosen after the primary cooler and before the electric tar precipitator. This is because the load on the blower is small at this time, and the electric tar precipitator is operated under positive pressure, which is relatively safe.

　　横管式初冷器

　　Horizontal tube primary cooler

　　焦化系统生产中煤气横管式初冷器主要结构是包括初冷器壳体、冷却管管束。横管式初冷器壳体是由钢板焊制而成的直立的长方形器体，壳体的前后两侧是初冷器的管板，管板外装有封头。在壳体侧面上、中部有喷洒液接管，顶部为煤气入口，底部有煤气出口。在横管式初冷器的操作中，除了冷却焦炉煤气外，在冷却器顶部及中部喷洒冷凝液，来吸收焦炉煤气中的萘，并冲刷掉冷却管上沉积的萘，从而有效的提高了传热效率。初冷器后的煤气含焦油和水的雾滴，在鼓风机的离心力作用下大部分以液态析出，余下部分在电捕焦油器的电场作用下沉淀下来。

　　In the production of coking system, the main structure of gas horizontal tube primary cooler is composed of primary cooler shell and cooling tube bundle. The shell of the horizontal tube primary cooler is an upright rectangular body welded from steel plates. The front and rear sides of the shell are the tube plates of the primary cooler, which are equipped with heads on the outside. There are spray nozzles on the side and middle of the shell, with a gas inlet at the top and a gas outlet at the bottom. In the operation of the horizontal tube primary cooler, in addition to cooling the coke oven gas, condensate is sprayed at the top and middle of the cooler to absorb naphthalene in the coke oven gas and flush out the naphthalene deposited on the cooling tube, effectively improving heat transfer efficiency. The gas after the primary cooler contains tar and water droplets, most of which precipitate in liquid form under the centrifugal force of the blower, and the remaining part precipitates under the electric field of the electric tar catcher.

　　初冷器后的粗煤气质量减少了2/3，而容积减少了3/5，从而减少了继续输送的电能消耗。

　　The quality of the crude gas after the primary cooler has decreased by 2/3, while the volume has decreased by 3/5, thereby reducing the consumption of electricity for continued transmission.

　　电捕焦油器

　　Electric tar catcher

　　电捕焦油器的沉淀管为沉淀极，与电流正极相接，电晕导线为电晕极，与电源负极相接，当导入高压直流电流后，两极之间形成非均匀电场，电晕极周围成为电晕区产生电晕现象，电晕极附近气体发生撞击电离现象，电晕区内煤气分子变策划能够带阳电离子和带阴电离子，电晕区外充满带负电荷的离子，它附与煤气中的焦油雾滴上，使焦油雾粒向沉淀管内壁上移动，沉淀壁面上，沿壁以重力下降到电捕焦油器底部，由于沉淀极是接地的，把电子导入地下，煤气离子重新变成中性分子，从器顶离开电捕焦油器。

　　The sedimentation tube of the electric tar catcher is the sedimentation electrode, which is connected to the positive electrode of the current, and the corona wire is the corona electrode, which is connected to the negative electrode of the power supply. When a high-voltage direct current is introduced, a non-uniform electric field is formed between the two electrodes. The corona phenomenon occurs around the corona electrode, and the gas near the corona electrode undergoes impact ionization. The gas molecules in the corona zone can carry positive and negative ions, while the gas outside the corona zone is filled with negatively charged ions, which attach to the tar droplets in the gas, causing the tar mist particles to move towards the inner wall of the sedimentation tube. On the sedimentation wall, they descend along the wall to the bottom of the electric tar catcher by gravity. Since the sedimentation electrode is grounded, electrons are introduced into the ground, and the gas ions become neutral molecules again. The top of the device leaves the electrostatic tar precipitator.

　　脱硫工段（HPF脱硫法）

　　Desulfurization section (HPF desulfurization method)

　　为什么要脱除煤气中的硫？

　　Why remove sulfur from coal gas?

　　煤气中硫的含量一般随炼焦煤中的含硫量而变，煤气中90%的硫以H2S形式存在，一般波动在4～10g/m3（煤气）。炼焦煤中含硫质量含量达1%，相当于煤气中H2S含量为10g/m3。HCN含量取决于煤中氮含量和炭化温度，一般为1～2.5g/m3（煤气）。H2S和HCN都是有毒化合物，H2S吸入人体后，轻则中毒，重则致人死亡。生产车间允许的H2S含量小于10g/m3。HCN毒性更大，人吸入50mg即可死亡。生产车间允许的HCN含量小于0.3mg/m3。H2S和HCN的水溶液也具有强烈的毒性，水中含HCN达0.04～0.1mg/kg可致鱼死亡。工厂排污水要求H2S和HCN的含量小于0.05mg/L。在煤气输送过程中会腐蚀设备和管道；作燃料燃烧时，生成SOx和NOx严重污染大气，甚至形成酸雨。焦炉煤气用在冶炼优质钢和供化学合成工业时，对H2S含量的要求更加严格，有的甚至要求小于1mg/m3。

　　The sulfur content in coal gas generally varies with the sulfur content in coking coal. 90% of the sulfur in coal gas exists in the form of H2S, which generally fluctuates between 4-10g/m3 (coal gas). The sulfur content in coking coal reaches 1%, which is equivalent to a H2S content of 10g/m3 in coal gas. The HCN content depends on the nitrogen content and carbonization temperature in coal, generally ranging from 1 to 2.5 g/m3 (coal gas). H2S and HCN are both toxic compounds. When H2S is inhaled into the human body, it can cause mild poisoning and severe death. The allowable H2S content in the production workshop is less than 10g/m3. HCN is more toxic, and humans can die by inhaling 50mg. The allowable HCN content in the production workshop is less than 0.3mg/m3. The aqueous solution of H2S and HCN also has strong toxicity, and the presence of HCN in water up to 0.04-0.1mg/kg can cause fish death. The factory requires the content of H2S and HCN in the wastewater to be less than 0.05mg/L. Corrosion of equipment and pipelines during gas transportation; When burned as fuel, SOx and NOx are generated, which seriously pollute the atmosphere and even form acid rain. When coke oven gas is used for smelting high-quality steel and supplying chemical synthesis industry, the requirements for H2S content are more stringent, and some even require less than 1mg/m3.

　　综上所述，焦炉煤气必须脱除H2S和HCN。另外还可以变废为宝，生产硫磺和硫酸等化工产品。

　　In summary, coke oven gas must remove H2S and HCN. In addition, it can also turn waste into treasure by producing chemical products such as sulfur and sulfuric acid.

　　1. 工艺流程

　　1. Process flow

　　脱硫装置是以煤气中的氨为碱源，HPF为催化剂的湿式氧化法脱硫工艺，再生为喷射再生方式。喷射再生槽设在脱硫塔上部。使用负压脱硫工艺。

　　The desulfurization device is a wet oxidation desulfurization process using ammonia in coal gas as the alkali source and HPF as the catalyst, with regeneration using jet regeneration. The jet regeneration tank is located at the upper part of the desulfurization tower. Use negative pressure desulfurization process.

　　为保证脱硫后煤气含H2S≤20mg/m3，脱硫装置采用HPF为催化剂的三塔串联设计。

　　To ensure that the H2S content in the desulfurized gas is ≤ 20mg/m3, the desulfurization unit adopts a three tower series design with HPF as the catalyst.

　　由鼓冷装置电捕来的煤气依次进入三个脱硫再生塔脱硫段。脱硫段顶喷淋下来的脱硫液逆流接触煤气以吸收煤气中的硫化氢（同时吸收煤气中的氨，以补充脱硫液中的碱源）。脱硫后煤气含硫化氢约20mg/m3，送入鼓风机室升压。

　　The gas captured by the drum cooling device enters the desulfurization sections of three desulfurization regeneration towers in sequence. The desulfurization solution sprayed from the top of the desulfurization section contacts the gas in reverse flow to absorb hydrogen sulfide in the gas (while absorbing ammonia in the gas to supplement the alkali source in the desulfurization solution). After desulfurization, the gas contains about 20mg/m3 of hydrogen sulfide and is sent to the blower room for boosting.

　　在脱硫再生塔脱硫段内吸收了H2S、HCN的脱硫液汇聚到塔底，然后用脱硫液泵送入脱硫再生塔顶部的再生段，通过再生段喷射器吸入空气使溶液在塔内得以氧化再生。再生后的溶液从塔顶经液位调节器自流回脱硫再生塔脱硫段，吸收煤气中的H2S、HCN。

　　The desulfurization solution that absorbs H2S and HCN in the desulfurization section of the desulfurization regeneration tower gathers at the bottom of the tower, and is then pumped into the regeneration section at the top of the desulfurization regeneration tower by the desulfurization solution pump. Air is sucked in through the regeneration section injector to oxidize and regenerate the solution inside the tower. The regenerated solution flows back to the desulfurization section of the desulfurization regeneration tower through the liquid level regulator at the top of the tower, absorbing H2S and HCN from the gas.

　　浮于脱硫再生塔顶部的硫磺泡沫，利用位差自流入泡沫槽，经硫泡沫泵送入超级离心机，超级离心机为逆流卧式螺旋卸料沉降离心机，转鼓转速3000rpm。分离出的硫饼含水≤35％，集于硫池中，定期收集外卖。滤液收入滤液槽，大部分滤液经滤液泵返回脱硫系统，为防止HPF脱硫装置NH4SCN、(NH4)2S2O3盐类积累，一部分滤液送往提盐单元提取盐类。

　　The sulfur foam floating on the top of the desulfurization regeneration tower flows into the foam tank automatically by potential difference and is pumped into the super centrifuge by the sulfur foam pump. The super centrifuge is a countercurrent horizontal spiral discharge sedimentation centrifuge, and the rotating speed of the drum is 3000 rpm. The separated sulfur cake has a water content of ≤ 35% and is collected in a sulfur pool for regular takeout collection. The filtrate is collected into the filtrate tank, and most of the filtrate is returned to the desulfurization system through the filtrate pump. To prevent the accumulation of NH4SCN and (NH4) 2S2O3 salts in the HPF desulfurization unit, a portion of the filtrate is sent to the salt extraction unit for salt extraction.

　　提盐单元为间歇操作，操作一釜为8小时。滤液由滤液原料槽抽入硫代硫酸氨蒸发器，用蒸汽加热浓缩。为防止温度过高，盐类分解，蒸发需在真空条件下进行，控制蒸发温度为90℃。待蒸发结束后，通过可旋转的溜槽将料液放至真空过滤器，热过滤出去(NH4)2CO3等杂质。滤渣在容渣槽内用滤液溶解后回脱硫系统。滤液至硫代硫酸氨结晶槽用夹套冷却水（低温水）冷至20℃左右，加入同种晶种使其结晶，最后在离心机中分离得到粗制硫代硫酸氨，用人工铲出，装入塑料袋作为产品出厂。

　　The salt extraction unit is operated intermittently, with one kettle operating for 8 hours. The filtrate is drawn from the filtrate raw material tank into the ammonium thiosulfate evaporator and concentrated by steam heating. To prevent excessive temperature and salt decomposition, evaporation needs to be carried out under vacuum conditions, and the evaporation temperature should be controlled at 90 ℃. After the evaporation is completed, the material liquid is placed into a vacuum filter through a rotatable chute, and impurities such as (NH4) 2CO3 are hot filtered out. The filter residue is dissolved in the filtrate in the slag tank and returned to the desulfurization system. The filtrate is cooled to around 20 ℃ in the ammonium thiosulfate crystallization tank using jacket cooling water (low-temperature water), and the same type of crystal seeds are added to crystallize it. Finally, crude ammonium thiosulfate is separated in a centrifuge and manually scooped out. The product is then placed in a plastic bag and shipped from the factory.

　　离心硫代硫酸氨后的滤液经中间槽压入硫氰酸氨原料槽，由此抽入硫氰酸氨蒸发器，用蒸汽加热浓缩，待蒸发结束后，通过可旋转的溜槽将料液放至真空过滤器，进一步除去(NH4)2CO3等杂质。滤渣在容渣槽内用滤液溶解后回脱硫系统。滤液至硫氰酸氨结晶槽用夹套冷却水（低温水）冷至30℃左右，加入同种晶种使其结晶，最后在离心机中分离得到粗制硫氰酸氨，用人工铲出，装入塑料袋作为产品出厂。离心滤液可回蒸发器循环套用。多次套用后，由于杂质逐渐积累，需定期送回脱硫液系统。

　　After centrifuging ammonium thiosulfate, the filtrate is pressed into the ammonium thiocyanate raw material tank through an intermediate tank, and then drawn into the ammonium thiocyanate evaporator for concentration by steam heating. After the evaporation is complete, the material liquid is placed into a vacuum filter through a rotatable chute to further remove impurities such as (NH4) 2CO3. The filter residue is dissolved in the filtrate in the slag tank and returned to the desulfurization system. The filtrate is cooled to around 30 ℃ in the ammonium thiocyanate crystallization tank using jacket cooling water (low-temperature water), and the same type of crystal seeds are added to crystallize it. Finally, crude ammonium thiocyanate is separated in a centrifuge and manually scooped out. The product is then placed in a plastic bag and shipped from the factory. The centrifugal filtrate can be recycled back to the evaporator for reuse. After multiple applications, due to the gradual accumulation of impurities, it is necessary to regularly return the desulfurization solution system.

　　从蒸发器蒸出的水汽进入蒸汽冷凝器，除水后，进入排气洗净塔与来自蒸氨装置的蒸氨废水逆流接触净化，不凝性气体经真空泵直排大气。

　　The water vapor evaporated from the evaporator enters the steam condenser, after removing water, it enters the exhaust cleaning tower and is purified by countercurrent contact with the ammonia wastewater from the ammonia distillation unit. Non condensable gases are directly discharged into the atmosphere through a vacuum pump.

　　经蒸汽冷凝器冷凝后的废水满流至液封槽，送回脱硫液系统。

　　The wastewater condensed by the steam condenser flows to the liquid seal tank and is sent back to the desulfurization liquid system.

　　2. 工艺特点

　　2. Process characteristics

　　1）采用以氨为碱源，HPF为催化剂的焦炉煤气脱硫脱氰新工艺，此法不但具有较高的脱硫脱氰效率，而且流程短，不需外加碱，催化剂用量少，操作费用低，一次性投资省。

　　1) A new process for desulfurization and decyanation of coke oven gas using ammonia as the base source and HPF as the catalyst is adopted. This method not only has high desulfurization and decyanation efficiency, but also has a short process, does not require additional alkali, requires less catalyst, has low operating costs, and saves one-time investment.

　　2）提盐工艺成熟可靠，技术先进，生产操作稳定，减少废液排放量，实现了变废为宝。

　　2) The salt extraction process is mature and reliable, with advanced technology, stable production operations, and reduced waste liquid emissions, achieving the goal of turning waste into treasure.

　　3. 主要技术操作指标

　　3. Main technical operation indicators

　　脱硫塔前煤气温度25～30℃

　　Gas temperature in front of desulfurization tower 25-30 ℃

　　脱硫塔后煤气温度30～35℃

　　Gas temperature after desulfurization tower is 30-35 ℃

　　脱硫再生塔底部脱硫液温度～35℃

　　Bottom desulfurization solution temperature of desulfurization regeneration tower~35 ℃

　　主要技术操作指标泡沫槽温度～35℃

　　Main technical operation index foam tank temperature~35 ℃

　　蒸发器温度～90℃

　　Evaporator temperature~90 ℃

　　硫代硫酸氨结晶槽温度～20℃

　　Temperature of ammonium thiosulfate crystallization tank~20 ℃

　　硫氰酸氨结晶槽温度～30℃

　　Temperature of ammonium thiocyanate crystallization tank~30 ℃

　　单台脱硫塔阻力1.5kPa

　　Resistance of a single desulfurization tower is 1.5kPa

　　真空泵前压力-30kPa

　　Front pressure of vacuum pump -30kPa

　　脱硫液组成：

　　Composition of desulfurization solution:

　　H.P.F含量0.1～0.2g/l

　　H. P.F content 0.1-0.2g/l

　　游离氨含量4～5g/l

　　Free ammonia content 4-5g/l

　　PH值8.3～8.5 g/l

　　PH value 8.3-8.5 g/l

　　悬浮硫含量1～1.2g/l

　　Suspended sulfur content 1-1.2g/l

　　脱硫后煤气含H2S≤20mg/m3

　　After desulfurization, the gas contains H2S ≤ 20mg/m3

　　4. 主要设备的工作原理

　　4. Working principle of main equipment

　　脱硫塔

　　desulfurization tower

　　自电捕焦油器出来的焦炉煤气进入第一级脱硫再生塔的脱硫段下部，并沿脱硫段自下而上与顶部喷洒的脱硫液逆流接触，将煤气中的大部分H2S吸收在脱硫液中。吸收了H2S后的脱硫液通过塔底由脱硫液循环泵泵至脱硫再生塔顶，通过喷射器与空气接触，进行氧化再生，再生的溶液经液位调节器自流到脱硫段顶部与煤气逆流接触，循环使用。从一级脱硫系统净化后的焦炉煤气依次进入第二级、第三级脱硫再生塔，其过程与一级脱硫相同。经过三级脱硫，煤气中的H2S含量可达到20mg/m3以下。

　　The coke oven gas from the electrostatic tar precipitator enters the lower part of the desulfurization section of the first stage desulfurization regeneration tower and comes into contact with the top sprayed desulfurization solution from bottom to top in reverse flow along the desulfurization section, absorbing most of the H2S in the gas into the desulfurization solution. After absorbing H2S, the desulfurization solution is pumped by the desulfurization solution circulation pump from the bottom of the tower to the top of the desulfurization regeneration tower. It is then subjected to oxidation regeneration by contact with air through an injector. The regenerated solution flows automatically to the top of the desulfurization section through a liquid level regulator and comes into contact with the gas in reverse flow, for recycling. The purified coke oven gas from the first stage desulfurization system enters the second and third stage desulfurization regeneration towers in sequence, following the same process as the first stage desulfurization. After three-stage desulfurization, the H2S content in the gas can reach below 20mg/m3.

　　为了保持一定的催化剂浓度并尽量减少其耗量，采用了连续补加少量催化剂的设施。

　　In order to maintain a certain concentration of catalyst and minimize its consumption, a facility of continuously adding a small amount of catalyst was adopted.

　　为了保证脱硫效果，采用向脱硫塔连续补充浓氨水。采用引射自吸式再生，硫泡沫自流入硫泡沫槽然后硫泡沫加工成硫磺或硫膏，再生后的脱硫液经液位调节器后自动流入脱硫段进行煤气脱硫生产，经自吸喷射器空气与脱硫液充分混合，发生氧化、再生反应.

　　To ensure the desulfurization effect, continuous supply of concentrated ammonia water is used to the desulfurization tower. The injection self-priming regeneration is adopted. The sulfur foam flows into the sulfur foam tank automatically, and then the sulfur foam is processed into sulfur or sulfur paste. The regenerated desulfurization liquid flows into the desulfurization section automatically after passing through the liquid level regulator for gas desulfurization production. The air of the self-priming injector is fully mixed with the desulfurization liquid, and oxidation and regeneration reactions occur

　　5. 主要环保措施

　　5. Main environmental protection measures

　　1） 各贮槽放散气体经压力平衡系统回吸煤气管道，废气不外排。

　　1) The gas released from each storage tank is sucked back into the gas pipeline through the pressure balance system, and the exhaust gas is not discharged outside.

　　2） 放空液进入地下放空槽，然后返回系统，不外排。

　　2) The emptying liquid enters the underground emptying tank and then returns to the system without being discharged externally.

　　3） 利用提盐工艺减少废液排放量，实现了变废为宝。

　　3) By utilizing the salt extraction process, the discharge of waste liquid has been reduced, achieving the goal of turning waste into treasure.

　　6、主要影响因素

　　6. Main influencing factors

　　脱硫塔的操作温度和压力：温度过高或压力过大会加速副反应的进行。

　　The operating temperature and pressure of the desulfurization tower: If the temperature or pressure is too high, it will accelerate the progress of side reactions.

　　脱硫液的pH值：脱硫液的pH值应维持在8.1～8.7之间，小于8.1反应慢，大于8.7副反应加剧。

　　The pH value of desulfurization solution: The pH value of desulfurization solution should be maintained between 8.1 and 8.7. If it is less than 8.1, the reaction will be slow, and if it is greater than 8.7, the side reactions will intensify.

　　还有，再生时间和脱硫剂用量等因素。

　　Also, factors such as regeneration time and desulfurizer dosage.

　　硫铵工段（喷淋式饱和器生产硫铵）

　　Ammonium sulfate section (spray saturator production of ammonium sulfate)

　　为什么要对煤气进行脱氨？

　　Why do we need to deamination coal gas?

　　煤热解温度高于500℃时形成氨，高温炼焦煤气中的氮约有20～25%转化为氨，粗煤气中氨含量为8～11g/m3（体积百分数1.0～1.5%）煤气中氨含量的8～16%在煤气冷却中溶于凝缩液中。残留于煤气中的氨大部分被终冷水吸收，在凉水塔喷洒冷却时又都解吸进入到大气，造成污染；由于煤气中的氨与氰化氢化合，形成溶解度高的复合物，从而加剧了腐蚀作用。

　　When the coal pyrolysis temperature is higher than 500 ℃, ammonia is formed. About 20-25% of the nitrogen in high-temperature coking gas is converted into ammonia. The ammonia content in crude gas is 8-11g/m3 (volume percentage 1.0-1.5%). 8-16% of the ammonia content in gas dissolves in the condensate during gas cooling. Most of the ammonia remaining in the gas is absorbed by the final cooling water, and when it is sprayed and cooled in the cooling tower, it is desorbed into the atmosphere, causing pollution; Due to the combination of ammonia and hydrogen cyanide in coal gas, a highly soluble complex is formed, which exacerbates the corrosion effect.

　　此外，煤气中的氨在燃烧时会生成有毒的、有腐蚀性的氧化氮；氨在粗苯回收中能使油和水形成稳定的乳化液，妨碍油水分离。上述这些都使现代化焦化生产遇到困难，为此，煤气中氨含量不允许超过0.03g/m3。

　　In addition, ammonia in coal gas generates toxic and corrosive nitrogen oxides during combustion; Ammonia can form a stable emulsion between oil and water in crude benzene recovery, which hinders oil-water separation. All of the above make modern coking production difficult. Therefore, the ammonia content in the gas is not allowed to exceed 0.03g/m3.

　　因此必须对煤气中的氨加以回收，目前中国大部分焦化厂采用硫酸自煤气中吸收氨，生产硫酸铵，作为化学肥料加以利用。

　　Therefore, it is necessary to recover ammonia from coal gas. Currently, most coking plants in China use sulfuric acid to absorb ammonia from coal gas, produce ammonium sulfate, and utilize it as a chemical fertilizer.

　　1. 工艺流程

　　1. Process flow

　　由煤气鼓风机送来的煤气经煤气预热器进入饱和器。煤气在饱和器的上段分两股入环形室经循环母液喷洒，其中的氨被母液中的硫酸吸收，然后煤气合并成一股进入后室经母液最后一次喷淋进饱和器内旋风式除酸器，以便分离煤气所夹带的酸雾，最后送至终冷洗苯装置。

　　The gas sent by the gas blower enters the saturator through the gas preheater. The gas is divided into two streams in the upper section of the saturator and sprayed into the annular chamber through the circulating mother liquor. The ammonia in the mother liquor is absorbed by the sulfuric acid in the mother liquor, and then the gas is combined into one stream and enters the rear chamber. The mother liquor is sprayed for the last time and enters the cyclone type acid remover in the saturator to separate the acid mist carried by the gas. Finally, it is sent to the final cold washing benzene unit.

　　饱和器下段上部的母液经母液循环泵连续抽出送至环形室喷洒，吸收了氨的循环母液由中心下降管流至饱和器下段的底部，在此晶核通过饱和介质向上运动，使晶体长大，并引起颗粒分级。用结晶泵将其底部的浆液送至结晶槽。饱和器满流口溢出的母液经满流槽流至母液贮槽，满流槽内含液封槽，满流槽底部的母液用小母液泵送入饱和器的后室喷淋。母液贮槽的母液用小母液泵送至满流槽。此外，母液贮槽还可供饱和器检修时贮存母液之用。

　　The mother liquor in the upper part of the lower section of the saturator is continuously pumped out by the mother liquor circulation pump and sent to the annular chamber for spraying. The circulating mother liquor that absorbs ammonia flows from the central downcomer to the bottom of the lower section of the saturator, where the crystal nuclei move upward through the saturated medium, causing crystal growth and particle classification. Use a crystallization pump to send the slurry at the bottom to the crystallization tank. The mother liquor overflowing from the full flow port of the saturator flows into the mother liquor storage tank through the full flow channel, which contains a liquid sealed tank. The mother liquor at the bottom of the full flow channel is pumped into the rear chamber of the saturator for spraying by a small mother liquor pump. The mother liquor from the mother liquor storage tank is pumped to the full flow tank using a small mother liquor pump. In addition, the mother liquor storage tank can also be used to store the mother liquor during the maintenance of the saturator.

　　结晶槽的浆液排放到离心机，经分离的硫铵由输送机送至振动流化床干燥机，并用被热风器加热的空气干燥，再经冷风冷却后进入硫铵贮斗，然后称量、包装送入成品库。

　　The slurry from the crystallization tank is discharged into a centrifuge, and the separated ammonium sulfate is transported by a conveyor to a vibrating fluidized bed dryer, where it is dried using air heated by a hot air blower. After being cooled by cold air, it enters the ammonium sulfate storage hopper, weighed, packaged, and sent to the finished product warehouse.

　　滤出的母液与结晶槽满流出来的母液一同自流回饱和器的下段。

　　The filtered mother liquor flows back to the lower section of the saturator together with the mother liquor flowing out from the crystallization tank.

　　干燥硫铵后的尾气在排入大气前设有两级除尘。首先经两组干式旋风除尘器除去尾气中夹带的大部分粉尘，再由尾气引风机抽送至尾气洗净塔，用尾气洗净塔泵对尾气进行连续循环喷洒，以进一步除去尾气中夹带的残留粉尘，最后经捕雾器除去尾气中夹带的液滴后排入大气。

　　The tail gas after drying ammonium sulfate is equipped with two-stage dust removal before being discharged into the atmosphere. Firstly, most of the dust carried in the exhaust gas is removed by two sets of dry cyclone dust collectors. Then, the exhaust gas is drawn to the exhaust gas cleaning tower by the exhaust gas induced draft fan, and the exhaust gas is continuously circulated and sprayed by the exhaust gas cleaning tower pump to further remove the residual dust carried in the exhaust gas. Finally, the liquid droplets carried in the exhaust gas are removed by the mist collector and discharged into the atmosphere.

　　油库来的硫酸送至硫酸高置槽，然后自流到满流槽。

　　The sulfuric acid from the oil depot is sent to the sulfuric acid high-level tank, and then flows automatically to the full flow tank.

　　2. 工艺特点

　　2. Process characteristics

　　1）采用喷淋式饱和器，集酸洗、除酸、结晶为一体，设备体积小，脱氨效率高，硫铵颗粒大，流程简单，工艺先进，技术可靠。

　　1) Adopting a spray type saturator, integrating acid washing, acid removal, and crystallization, the equipment has a small volume, high deamination efficiency, large ammonium sulfate particles, simple process, advanced technology, and reliable technology.

　　2）喷淋饱和器系统阻力小，鼓风机能耗低。

　　2) The spray saturator system has low resistance and low energy consumption of the blower.

　　3）硫铵母液系统设备及管道均采用超低碳不锈钢材质，使用寿命长，可保证装置长期连续稳定操作，减少维护费用。

　　3) The equipment and pipelines of the ammonium sulfate mother liquor system are made of ultra-low carbon stainless steel material, which has a long service life and can ensure long-term continuous and stable operation of the device, reducing maintenance costs.

　　4）硫铵干燥采用振动流化床，干燥效果好，易于操作维护。

　　4) Ammonium sulfate drying adopts a vibrating fluidized bed, which has good drying effect and is easy to operate and maintain.

　　5）干燥尾气采用干式及湿式两级除尘，除尘效率高，尾气中无粉尘夹带。

　　5) Dry exhaust gas adopts two-stage dust removal methods of dry and wet, with high dust removal efficiency and no dust entrainment in the exhaust gas.

　　3. 主要技术操作指标

　　3. Main technical operation indicators

　　饱和器后煤气含氨≤0.05g/m3

　　Ammonia content in gas after saturator ≤ 0.05g/m3

　　饱和器后煤气温度～55℃

　　Gas temperature after saturator~55 ℃

　　干燥后硫铵含水≤0.3%

　　After drying, the moisture content of ammonium sulfate is ≤ 0.3%

　　饱和器的阻力≤2kPa

　　The resistance of the saturator is ≤ 2kPa

　　4. 主要环保措施

　　4. Main environmental protection measures

　　1）放空母液进入地下放空槽，然后返回系统，不外排。

　　1) The emptying mother liquor enters the underground emptying tank and then returns to the system without being discharged.

　　2）硫铵干燥尾气采用干式及湿式两级除尘，无粉尘夹带。

　　2) The tail gas of ammonium sulfate drying adopts two-stage dry and wet dust removal, without dust entrainment.

　　5.主要设备的工作原理

　　5. Working principle of main equipment

　　喷淋式饱和器

　　Spray saturator

　　煤气经电捕焦油、脱硫并经鼓风机增压后进入煤气预热器，预热到60～70℃，目的是蒸出饱和器中水分，防止母液稀释。煤气由饱和器的中央气管经泡沸伞穿过母液层鼓泡而出，其中的氨被硫酸吸收，形成硫酸铵。在出酸器中分离出携带的液滴后，去粗苯回收工段。饱和器后煤气含氨量一般要求小于0.03g/m3。

　　The gas is subjected to electric tar capture, desulfurization, and pressurized by a blower before entering the gas preheater, which is preheated to 60-70 ℃ to evaporate the water in the saturator and prevent dilution of the mother liquor. Gas is bubbled out from the central gas pipe of the saturator through the mother liquor layer through a bubbling umbrella, and the ammonia in it is absorbed by sulfuric acid to form ammonium sulfate. After separating the carried droplets in the acid extractor, they are sent to the crude benzene recovery section. The ammonia content in the gas after saturator is generally required to be less than 0.03g/m3.

　　饱和器中母液经水封管进入满流槽，由此用泵打回到饱和器的底部，这样构成母液循环系统，并在器内形成上升的母液流。硫酸铵结晶沉于饱和器的锥底部，用泵把浆液送回到结晶槽，在此从浆液中沉淀出硫酸铵结晶，结晶槽满流液又回到饱和器。

　　The mother liquor in the saturator enters the full flow channel through a water sealed pipe, and is pumped back to the bottom of the saturator, forming a mother liquor circulation system and an upward mother liquor flow inside the saturator. Ammonium sulfate crystals settle at the bottom of the saturator cone, and the slurry is pumped back to the crystallization tank, where ammonium sulfate crystals precipitate from the slurry. The crystallization tank is filled with liquid and returns to the saturator.

　　硫酸铵结晶浆液在离心机分出结晶，结晶含水分1%～2%，在干燥器中脱水后送去仓库。

　　The ammonium sulfate crystallization slurry is separated into crystals in a centrifuge, with a moisture content of 1% to 2%. After dehydration in a dryer, it is sent to the warehouse.

　　6.主要影响因素

　　6. Main influencing factors

　　母液酸度：

　　Mother liquor acidity:

　　氨吸收设备内母液的酸度，主要影响硫酸铵结晶的粒度。随着母液酸度的提高，结晶平均粒度下降，另外，随着酸度的提高，母液黏度增大，增加了硫酸铵分子的扩散阻力，阻碍了晶体正常的成长。

　　The acidity of the mother liquor in the ammonia absorption equipment mainly affects the particle size of ammonium sulfate crystals. As the acidity of the mother liquor increases, the average crystal size decreases. In addition, with the increase of acidity, the viscosity of the mother liquor increases, which increases the diffusion resistance of ammonium sulfate molecules and hinders the normal growth of crystals.

　　母液温度：

　　Mother liquor temperature:

　　母液温度影响晶体的生长速度。通常晶体的生长速度随母液温度的升高而增大，且由于晶体各棱面对平均生成速度比晶体沿长向生长速度增长较快，故提高温度有助于降低长宽比而形成较好的晶体。但温度也不宜过高，过高想成局部过饱和现象，促使大量晶核形成。一般母液温度控制在50～55℃。

　　The temperature of the mother liquor affects the growth rate of crystals. The growth rate of crystals usually increases with the temperature of the mother liquid, and because the average generation rate of each facet of the crystal increases faster than the growth rate of the crystal along the longitudinal direction, increasing the temperature helps to reduce the aspect ratio and form better crystals. But the temperature should not be too high, as it may cause local supersaturation and promote the formation of a large number of crystal nuclei. The temperature of the mother liquor is generally controlled between 50-55 ℃.

　　母液循环：

　　Mother liquor circulation:

　　母液循环循环的目的是使器内的母液得到充分的搅拌，以提高传质速率。同时尽量使器内的母液酸度和温度均匀有利于晶核长大。

　　The purpose of mother liquor circulation is to thoroughly stir the mother liquor in the reactor to improve the mass transfer rate. At the same time, try to make the acidity and temperature of the mother liquor in the reactor uniform, which is beneficial for the growth of crystal nuclei.

　　另外，还有晶比和杂质的影响：晶比是指悬浮于母液中硫酸铵结晶的体积对母液总体积的百分比。母液中的杂质对晶体生长有抑制作用。

　　In addition, there are also effects of crystal ratio and impurities: crystal ratio refers to the percentage of the volume of ammonium sulfate crystals suspended in the mother liquor to the total volume of the mother liquor. Impurities in the mother liquor have an inhibitory effect on crystal growth.

　　终冷洗苯工段

　　Final cold washing benzene section

　　煤气进入吸苯塔前为什么要进行最终冷却？

　　Why is final cooling necessary before gas enters the benzene absorption tower?

　　粗苯回收主要影响因素之一就是回收温度。煤气中苯属烃的含量一定时，如果洗油吸收苯的吸收温度较低，吸收推动力增大，苯回收率增加。实践证明，最适宜的温度是20～28℃。但煤气经过饱和器后，温度一般为50～65℃。为了有效地利用洗油吸收煤气中的粗苯，必须进行煤气的最终冷却。

　　One of the main influencing factors for crude benzene recovery is the recovery temperature. When the content of benzene hydrocarbons in coal gas is constant, if the absorption temperature of benzene by wash oil is low, the absorption driving force increases, and the benzene recovery rate increases. Practice has proven that the most suitable temperature is 20-28 ℃. But after passing through the saturator, the temperature of the gas is generally 50-65 ℃. In order to effectively utilize wash oil to absorb crude benzene in coal gas, it is necessary to perform final cooling of the gas.

　　1、工艺流程

　　1. Process flow

　　从硫铵装置来的约55℃的煤气，首先进入终冷塔，煤气分2段冷却。下段用约37℃循环冷却水，上段用约24℃循环冷却水将煤气冷到～25℃后进入洗苯塔，煤气经贫油洗涤脱除粗苯并经捕雾后，送往用户。

　　The gas at approximately 55 ℃ from the ammonium sulfate plant first enters the final cooling tower, where it is cooled in two stages. The lower section uses circulating cooling water at about 37 ℃, and the upper section uses circulating cooling water at about 24 ℃ to cool the gas to about 25 ℃ before entering the benzene washing tower. The gas is washed with lean oil to remove crude benzene and then sent to the user after mist capture.

　　终冷塔下段的循环冷却水从塔中部进入终冷塔下段，与煤气逆向接触冷却煤气后用泵抽出，经下段循环喷洒液冷却器，用循环水冷却到37℃进入终冷塔中部循环使用。终冷塔上段的循环冷却水从塔顶部进入终冷塔上段冷却煤气后用泵抽出，经上段循环喷洒液冷却器，用低温水冷却到24℃进入终冷塔顶部循环使用。同时，在终冷塔上段加入一定量的碱液，进一步脱除煤气中的H2S，保证煤气中的H2S含量≤20mg/m3。下段排出的冷凝液送至酚氰废水处理，上段排出的含碱冷凝液送至蒸氨装置蒸氨塔顶，分解剩余氨水中的固定铵。

　　The circulating cooling water in the lower section of the final cooling tower enters the lower section of the final cooling tower from the middle of the tower, cools the gas in reverse contact with it, and is pumped out. It then passes through the circulating spray liquid cooler in the lower section and is cooled to 37 ℃ by circulating water before entering the middle section of the final cooling tower for circulation. The circulating cooling water in the upper section of the final cooling tower enters the cooling gas in the upper section of the final cooling tower from the top of the tower and is pumped out. After passing through the upper section circulating spray liquid cooler, it is cooled to 24 ℃ with low-temperature water and enters the top of the final cooling tower for circulation. At the same time, a certain amount of alkaline solution is added to the upper section of the final cooling tower to further remove H2S from the gas, ensuring that the H2S content in the gas is ≤ 20mg/m3. The condensate discharged from the lower section is sent to the phenol cyanide wastewater treatment, while the alkaline condensate discharged from the upper section is sent to the top of the ammonia distillation unit to decompose the fixed ammonium in the remaining ammonia water.

　　由粗苯蒸馏装置送来的贫油从洗苯塔的顶部喷洒，与煤气逆向接触吸收煤气中的苯，塔底富油经富油泵送至粗苯蒸馏工段脱苯后循环使用。系统消耗的洗油，定期从洗油槽经富油泵入口补入系统。

　　The lean oil sent from the crude benzene distillation unit is sprayed from the top of the benzene washing tower, which comes into reverse contact with the gas to absorb benzene in the gas. The rich oil at the bottom of the tower is pumped by the rich oil pump to the crude benzene distillation section for benzene removal and recycling. The wash oil consumed by the system is regularly replenished into the system through the rich oil pump inlet from the wash oil tank.

　　2、工艺特点

　　2. Process characteristics

　　1）终冷采用直冷空喷形式，基建投资少。

　　1) The final cooling adopts a direct cooling air spray form, which requires less infrastructure investment.

　　2）煤气终冷采用闭路循环连续排污工艺，既减少污水排放量，又达到保护大气环境的目的。

　　2) The gas final cooling adopts a closed-loop continuous sewage discharge process, which not only reduces the amount of sewage discharge, but also achieves the goal of protecting the atmospheric environment.

　　3、主要技术操作指标

　　3. Main technical operation indicators

　　出终冷塔的煤气温度25～27℃

　　The temperature of the gas exiting the final cooling tower is 25-27 ℃

　　进洗苯塔的贫油温度27～29℃

　　The lean oil temperature entering the benzene washing tower is 27-29 ℃

　　终冷塔阻力＜1.5kPa

　　Final cooling tower resistance ＜ 1.5kPa

　　洗苯塔阻力＜1.5kPa

　　The resistance of the benzene washing tower is less than 1.5kPa

　　洗苯塔后煤气含苯量～4g/m3

　　The benzene content in the gas after washing the benzene tower is about 4g/m3

　　4、主要环保措施

　　4. Main environmental protection measures

　　系统内的放空水、放空油集中回收进入地下放空槽，然后返回系统，不外排。

　　The emptying water and oil in the system are collected and recycled into the underground emptying tank, and then returned to the system without being discharged.

　　5、主要设备的工作原理

　　5. Working principle of main equipment

　　终冷塔

　　Final cooling tower

　　终冷塔为隔板式塔分两段，下段用从凉水塔来的循环水喷淋，将煤气冷却至40℃左右，上段用温度为20～23℃的低温循环水喷淋，将煤气再冷却至25℃左右。热水丛终冷塔底部经水封管流到热水池，然后用泵送至凉水塔，经制冷机冷却后自流入冷水池，再用泵送到终冷塔下段。

　　The final cooling tower is a partition tower divided into two sections. The lower section is sprayed with circulating water from the cooling tower to cool the gas to around 40 ℃, while the upper section is sprayed with low-temperature circulating water at a temperature of 20-23 ℃ to further cool the gas to around 25 ℃. The bottom of the hot water bundle final cooling tower flows through a water seal pipe to the hot water tank, and then is pumped to the cooling tower. After being cooled by the refrigeration machine, it flows into the cold water tank and is then pumped to the lower section of the final cooling tower.

　　洗苯塔

　　Benzene washing tower

　　填料洗苯塔：填料分布在塔板上形成了煤气的曲折通道，增加了煤气的停留时间，同时增加了苯的吸收率。为了保证洗油在塔内的截面上均匀分布，在塔内每隔一定距离安装一块带有煤气涡流罩的液体再分布板。煤气涡流罩按同心圆排列在液体再分布板上，弯管出口方向与圆周相切，在同一圆周上的出口方向一致，相邻两圆周上的方向相反。由于弯管的导向作用，煤气流出涡流罩时，形成多股上升的旋风气流，因而使煤气得到混合，以均一的浓度进入上段填料。汇集在液体再分布板上的洗油，经升气管内的弯管流到设于升气管中心的圆棒表面，再流到下端的齿形圆板上，借重力喷溅成液滴而淋洒到下段填料上。从而可消除洗油沿塔壁下流及分布不均的现象。

　　Packing benzene washing tower: The packing is distributed on the tray to form a tortuous channel for gas, increasing the residence time of gas and increasing the absorption rate of benzene. In order to ensure uniform distribution of wash oil on the cross-section inside the tower, a liquid redistribution plate with a gas vortex hood is installed at regular intervals inside the tower. The gas vortex hood is arranged in concentric circles on the liquid redistribution plate, with the outlet direction of the bent pipe tangent to the circumference. The outlet direction on the same circumference is consistent, while the directions on adjacent circumferences are opposite. Due to the guiding effect of the bent pipe, when the gas flows out of the vortex hood, multiple upward swirling airflows are formed, which mix the gas and enter the upper packing at a uniform concentration. The wash oil collected on the liquid redistribution plate flows through the curved pipe in the riser to the surface of the circular rod located at the center of the riser, and then flows onto the toothed circular plate at the lower end, where it splashes into droplets by gravity and drips onto the lower filling material. This can eliminate the phenomenon of washing oil flowing down and unevenly distributed along the tower wall.

　　6、洗苯的主要影响因素

　　6. The main influencing factors of benzene washing

　　吸收温度：

　　Absorption temperature:

　　当煤气中苯族烃的含量一定时，温度愈低，洗油中与其平衡的粗苯含量愈高。

　　When the content of benzene hydrocarbons in coal gas is constant, the lower the temperature, the higher the content of crude benzene in the wash oil that is in equilibrium with it.

　　洗油的吸收能力及循环油量：

　　Absorption capacity and circulating oil volume of wash oil:

　　在其他条件一定时，洗油的相对分子质量减小将使洗油中粗苯含量增大，即吸收能力提高。增加洗油循环量可降低洗油中粗苯的含量，增加吸收推动力，从而可提高粗苯回收率。

　　When other conditions are constant, a decrease in the relative molecular weight of the wash oil will increase the content of crude benzene in the wash oil, that is, the absorption capacity will be improved. Increasing the circulation of wash oil can reduce the content of crude benzene in the wash oil, increase the absorption driving force, and thus improve the recovery rate of crude benzene.

　　贫油含苯量：

　　Poor oil benzene content:

　　贫油含苯量是决定塔后煤气含苯族烃量的主要因素之一。此外还有，如吸收表面积、煤气压力和流速等影响因素。

　　The benzene content in lean oil is one of the main factors determining the benzene hydrocarbon content in the gas after the tower. In addition, there are influencing factors such as absorption surface area, gas pressure, and flow rate.

　　7、洗油的质量要求

　　7. Quality requirements for washing oil

　　为满足从煤气中回收和制取粗苯的要求，洗油应具备如下性能：

　　To meet the requirements for recovering and producing crude benzene from coal gas, wash oil should have the following properties:

　　1）常温下对苯族烃有良好的吸收能力，在加热时又能使苯族烃很好地分离出来；

　　1) At room temperature, it has good absorption capacity for benzene hydrocarbons, and when heated, it can effectively separate benzene hydrocarbons;

　　2）具有化学稳定性，记在长期使用中吸收能力基本稳定；

　　2) Has chemical stability and has a stable absorption capacity over long-term use;

　　3）在吸收操作温度下不应析出固体沉淀物；

　　3) Solid precipitates should not precipitate at the absorption operating temperature;

　　4）易与水分离，且不生成乳化物；

　　4) Easy to separate from water and does not generate emulsions;

　　5）有较好的流动性，已于用泵抽送并能在填料上均匀分布。

　　5) Has good fluidity, can be pumped and evenly distributed on the packing.

　　焦化厂用于吸苯的主要焦油洗油和石油洗油。

　　The main tar wash oil and petroleum wash oil used for benzene absorption in coking plants.

　　焦油洗油是高温煤焦油中230～300℃的馏分，要求萘含量小于13%，焦油中含有一定数量的萘，有助于降低从洗油中析出沉淀物的温度。

　　Tar wash oil is a fraction of high-temperature coal tar at 230-300 ℃, with a naphthalene content of less than 13%. Tar contains a certain amount of naphthalene, which helps to reduce the temperature at which precipitates precipitate from the wash oil.

　　石油洗油系指轻柴油，为石油精馏时，在馏出汽油和煤油后所切取的馏分。（270～350℃的馏分，C9～C14）生产实践表明：用石油洗油苯，具有洗油耗量低、油水分离容易记忆操作等优点。石油洗油脱萘能力强，洗苯能力弱，故循环量大，蒸汽耗量也大。

　　Petroleum wash oil refers to light diesel oil, which is a fraction obtained by distilling gasoline and kerosene during petroleum distillation. The production practice of (270-350 ℃ fraction, C9-C14) shows that using petroleum to wash benzene oil has the advantages of low washing oil consumption and easy memory operation for oil-water separation. Petroleum washing has strong naphthalene removal ability and weak benzene washing ability, resulting in a large circulation volume and high steam consumption.

　　蒸氨装置

　　Ammonia evaporation device

　　1、工艺流程

　　1. Process flow

　　剩余氨水处理量按30 m3/h设计。

　　The remaining ammonia water treatment capacity is designed at 30 m3/h.

　　剩余氨水与蒸氨塔底排出的蒸氨废水换热后进入蒸氨塔，蒸氨塔底的一部分蒸氨废水经蒸汽再沸器用蒸汽加热后流回蒸氨塔并闪蒸产生蒸汽。塔顶同时加入从终冷塔上段排出的含碱冷凝液以分解剩余氨水中固定氨。蒸氨塔顶部的氨汽经分缩器和氨汽冷凝冷却器冷凝冷却后变成浓氨水，进入脱硫装置脱硫再生塔。换热后的蒸氨废水进入废水冷却器冷却后送至酚氰废水处理站。

　　The remaining ammonia water exchanges heat with the ammonia distillation wastewater discharged from the bottom of the ammonia distillation tower and enters the ammonia distillation tower. A portion of the ammonia distillation wastewater at the bottom of the ammonia distillation tower is heated with steam by a steam reboiler and flows back to the ammonia distillation tower to flash produce steam. Simultaneously add alkaline condensate discharged from the upper section of the final cooling tower to the top of the tower to decompose the remaining ammonia water and fix ammonia. The ammonia vapor at the top of the ammonia distillation tower is condensed and cooled by the condenser and ammonia vapor condenser to become concentrated ammonia water, which enters the desulfurization regeneration tower of the desulfurization unit. After heat exchange, the steam ammonia wastewater enters the wastewater cooler for cooling and is sent to the phenol cyanide wastewater treatment station.

　　2、工艺特点

　　2. Process characteristics

　　1）蒸氨塔采用不锈钢浮阀塔，操作稳定，蒸馏效率高，使用年限长。

　　1) The ammonia distillation tower adopts a stainless steel float valve tower, which has stable operation, high distillation efficiency, and long service life.

　　2）蒸氨塔分缩器采用钛材质，耐腐蚀。

　　2) The ammonia distillation tower condenser is made of titanium material, which is corrosion-resistant.

　　3、主要技术操作指标

　　3. Main technical operation indicators

　　蒸氨塔顶温度96℃

　　Ammonia distillation tower top temperature 96 ℃

　　蒸氨塔底压力0.03～0.04MPa

　　Bottom pressure of ammonia distillation tower 0.03-0.04MPa

　　废水冷却器后蒸氨废水的温度40℃

　　The temperature of the ammonia wastewater after the wastewater cooler is 40 ℃

　　4、主要设备的工作原理

　　4. Working principle of main equipment

　　蒸氨塔：

　　Ammonia distillation tower:

　　剩余氨水由塔上部第三板加入，沿各层塔板流下来的氨水与从塔底层送入的直接汽相接触。水蒸气经泡罩齿隙沸腾穿越塔板上的氨水层，形成鼓泡现象。在塔板上氨水与蒸汽相遇被加热至沸点，水中的氨、二氧化碳、硫化氢等随气体上升逐步转入气体中，这样的过程一直进行到塔底为止，最后由塔底排出的废水含氨量小于0.1g/L时，。当剩余氨水为混合氨水，入塔温度为60~70℃时，则每立方米氨水的直接蒸汽耗量为200Kg左右。

　　The remaining ammonia water is added from the third plate at the top of the tower, and the ammonia water flowing down along each layer of the tower plate comes into contact with the direct vapor phase sent from the bottom of the tower. Water vapor boils through the gaps between the bubble hood teeth and passes through the ammonia layer on the tray, forming a bubbling phenomenon. On the tray, ammonia water meets steam and is heated to boiling point. Ammonia, carbon dioxide, hydrogen sulfide, and other substances in the water gradually enter the gas as it rises. This process continues until the bottom of the tower, and finally when the ammonia content in the wastewater discharged from the bottom of the tower is less than 0.1g/L,. When the remaining ammonia water is mixed ammonia water and the inlet temperature is 60-70 ℃, the direct steam consumption per cubic meter of ammonia water is about 200kg.

　　氨分缩器

　　Ammonia separator

　　由蒸氨塔逸出的气体混合物中的硫化氢、氰化物等对普通钢管具有强烈的腐蚀作用，故目前多采用铸铁管埋入式分缩器。在分缩器中氨气走管内，冷却水走管外。此种分缩器耐酸性较好，使用寿命较长，但较笨重。

　　The hydrogen sulfide, cyanide, and other substances in the gas mixture released from the ammonia distillation tower have a strong corrosive effect on ordinary steel pipes, so cast iron pipe buried type reducers are currently commonly used. In the splitter, ammonia gas flows through the tube and cooling water flows through the tube. This type of splitter has good acid resistance and a long service life, but it is relatively bulky.

　　5、主要环保措施

　　5. Main environmental protection measures

　　放空液进入地下放空槽，然后返回系统，不外排。

　　The emptying liquid enters the underground emptying tank and then returns to the system without being discharged externally.

　　粗苯蒸馏工段

　　Crude benzene distillation section

　　为什么要对粗苯进行回收？

　　Why recycle crude benzene?

　　粗苯是多种碳氢化合物组成的复杂混合物。粗苯本身用途不大。但由粗苯精制出的苯、甲苯、二甲苯、三甲苯等组分，是生产黄色炸药、塑料等的重要原料。此外还含有不饱和化合物、硫化物、饱和烃、酚类和砒啶碱类。粗苯的产率一般为干基配合煤料的0.75%~1.1%，因此从炭化室逸出的煤气含粗苯为28~35g/m3。

　　Crude benzene is a complex mixture composed of multiple hydrocarbons. Crude benzene itself has little practical use. But the components such as benzene, toluene, xylene, and trimethylbenzene refined from crude benzene are important raw materials for the production of yellow explosives, plastics, etc. In addition, it also contains unsaturated compounds, sulfides, saturated hydrocarbons, phenols, and arsenic bases. The yield of crude benzene is generally 0.75% to 1.1% of the dry coal feed, so the gas escaping from the carbonization chamber contains 28~35g/m3 of crude benzene.

　　粗苯的各主要组分均在180℃前馏出，180℃后的馏出物成为溶剂油。在测定粗苯中的各组分的含量和计算产量时，通常将180℃前馏出馏出量当作100%来计算，故以其180℃前馏出馏出量作为鉴别粗苯质量的指标之一。粗苯在180℃前馏出馏出量取决于粗苯工段的工艺流程和操作制度。180℃前馏出馏出量愈多，粗苯质量愈好。一般要求粗苯在180℃前馏出馏出量为93%～95%。

　　The main components of crude benzene are distilled before 180 ℃, and the distillate after 180 ℃ becomes solvent oil. When determining the content of each component in crude benzene and calculating the yield, the distillation yield before 180 ℃ is usually calculated as 100%. Therefore, the distillation yield before 180 ℃ is used as one of the indicators to identify the quality of crude benzene. The amount of crude benzene distilled before 180 ℃ depends on the process flow and operating system of the crude benzene section. The more distillate is produced before 180 ℃, the better the quality of crude benzene. Generally, it is required that the crude benzene be distilled off at 93% to 95% before 180 ℃.

　　1、工艺流程

　　1. Process flow

　　从终冷洗苯装置送来的富油依次送经油汽换热器、贫富油换热器，再经管式炉加热至190℃后进入脱苯塔，在此用再生器来的直接蒸汽进行汽提和蒸馏。塔顶逸出的粗苯蒸汽经油汽换热器、粗苯冷凝冷却器后，进入油水分离器。分出的粗苯送入粗苯回流槽，部分用粗苯回流泵送至塔顶作为回流，其余进入粗苯中间槽，再用粗苯产品泵送至油库。

　　The rich oil sent from the final cold washing benzene unit is sequentially sent through the oil steam heat exchanger, the rich and poor oil heat exchanger, and then heated to 190 ℃ in the tube furnace before entering the benzene removal tower, where direct steam from the regenerator is used for stripping and distillation. The crude benzene vapor escaping from the top of the tower enters the oil-water separator after passing through the oil vapor heat exchanger and crude benzene condenser. The separated crude benzene is sent to the crude benzene reflux tank, some of which are pumped to the top of the tower as reflux by the crude benzene reflux pump, while the rest enter the crude benzene intermediate tank and are then pumped to the oil depot by the crude benzene product pump.

　　脱苯塔底贫油槽排出的贫油，用热贫油泵经贫富油换热器和一、二段贫油冷却器冷却至27～29℃后去终冷洗苯装置。

　　The lean oil discharged from the bottom lean oil tank of the benzene removal tower is cooled to 27-29 ℃ by a hot lean oil pump through a lean rich oil heat exchanger and first and second stage lean oil coolers before being sent to the final cold washing benzene unit.

　　在脱苯塔的顶部设有断塔盘及塔外油水分离器，以引出塔顶积水，稳定操作。

　　At the top of the benzene removal tower, there is a broken tray and an external oil-water separator to remove the accumulated water at the top of the tower and ensure stable operation.

　　在脱苯塔侧线引出萘油馏份，以降低贫油含萘。引出的萘油馏份进入残渣槽。

　　Extract naphthalene oil fraction from the side line of the benzene removal tower to reduce the naphthalene content in lean oil. The extracted naphthalene oil fraction enters the residue tank.

　　为保证洗油质量，从热贫油泵来的贫油引出1～1.5%的富油，送入再生塔内，用经管式炉过热的蒸汽蒸吹再生。再生残渣排入残渣槽，用泵送至油库装置。

　　To ensure the quality of the washing oil, 1-1.5% of the rich oil is extracted from the lean oil pump and sent into the regeneration tower for regeneration using superheated steam from a tube furnace. The regenerated residue is discharged into the residue tank and pumped to the oil storage facility.

　　各油水分离器排出的分离水，经控制分离器排入分离水槽，用泵送往冷凝鼓风装置剩余氨水槽。

　　The separated water discharged from each oil-water separator is controlled to be discharged into the separation water tank and pumped to the remaining ammonia water tank of the condensing blower device.

　　各贮槽的不凝气集中引至吸煤气管道。

　　The non condensable gas from each storage tank is concentrated and led to the gas suction pipeline.

　　2、工艺特点

　　2. Process characteristics

　　1）脱苯塔上段设有断塔板，防止塔板积水，利于脱苯塔的操作。

　　1) The upper section of the benzene removal tower is equipped with a broken tray to prevent water accumulation and facilitate the operation of the benzene removal tower.

　　2）管式炉炉管采用不锈钢材质。

　　2) The tube furnace tube is made of stainless steel material.

　　3） 贫富油换热器和油汽换热器采用不锈钢材质。

　　3) The rich poor oil heat exchanger and oil vapor heat exchanger are made of stainless steel material.

　　4） 各贮槽放散气体经压力平衡系统回吸煤气管道，废气不外排。

　　4) The gas released from each storage tank is sucked back into the gas pipeline through the pressure balance system, and the exhaust gas is not discharged outside.

　　3、 主要技术操作指标

　　3. Main technical operation indicators

　　管式加热炉后富油温度190℃

　　Rich oil temperature after tube heating furnace 190 ℃

　　脱苯塔顶部温度92℃

　　The top temperature of the benzene removal tower is 92 ℃

　　脱苯塔底部贫油温度185℃

　　The lean oil temperature at the bottom of the benzene removal tower is 185 ℃

　　入再生器过热蒸气温度400℃

　　The temperature of superheated steam entering the regenerator is 400 ℃

　　二段贫油冷却器后贫油温度27～29℃

　　The lean oil temperature after the two-stage lean oil cooler is 27-29 ℃

　　脱苯塔底部压力0.04MPa

　　Bottom pressure of benzene removal tower 0.04MPa

　　再生塔顶部压力0.05MPa

　　Regeneration tower top pressure 0.05MPa

　　4、 主要环保措施

　　4. Main environmental protection measures

　　1）各贮槽放散气体经压力平衡系统回吸煤气管道，废气不外排。

　　1) The gas released from each storage tank is sucked back into the gas pipeline through the pressure balance system, and the exhaust gas is not discharged outside.

　　2）系统内的放空水、放空油和漏液集中回收进入地下放空槽，然后返回系统，不外排。

　　2) The vented water, vented oil, and leaked liquid in the system are collected and recycled into the underground venting tank, and then returned to the system without being discharged.

　　5、主要设备的工作原理

　　5. Working principle of main equipment

　　管式炉

　　tubular furnace

　　管式炉有圆筒体的辐射室、长方体的对流室和烟囱三大部分组成。沿炉管的长度方向，热强度的分布是不均匀的。一般小的圆筒炉，在辐射室上方设有一个由高铬镍合金钢制成的辐射锥，它的辐射作用，可使炉管上部的热强度提高，从而使炉管沿长度方向的受热比较均匀。

　　A tube furnace consists of three main parts: a cylindrical radiation chamber, a rectangular convection chamber, and a chimney. The distribution of thermal intensity along the length of the furnace tube is uneven. A generally small cylindrical furnace is equipped with a radiation cone made of high chromium nickel alloy steel above the radiation chamber. Its radiation effect can increase the thermal intensity of the upper part of the furnace tube, thereby making the heating of the furnace tube along the length direction more uniform.

　　对流室置于辐射室之上，对流管水平放。其中紧靠辐射段的两排横管为过热蒸汽管，用于将脱苯用的直接蒸汽过热至400℃以上。其余各排管用于富油的初步加热。

　　The convection chamber is placed above the radiation chamber, and the convection tube is placed horizontally. The two rows of horizontal pipes adjacent to the radiation section are superheated steam pipes, used to overheat the direct steam used for benzene removal to above 400 ℃. The remaining pipes are used for preliminary heating of the rich oil.

　　温度为130℃左右的富油分两程先进入对流段，加热到180～200℃后再去脱苯塔。

　　The rich oil with a temperature of around 130 ℃ enters the convection section in two stages, and is heated to 180-200 ℃ before going to the benzene removal tower.

　　再生器

　　a regenerator

　　洗油再生器中部设有带分布装置的进料管，下部设有残渣排出管。为了降低洗油的蒸出温度，再生器底部设有直接蒸汽管，通入脱苯蒸馏所需的绝大部分或全部蒸汽。

　　There is a feed pipe with a distribution device in the middle of the wash oil regenerator, and a residue discharge pipe in the lower part. In order to reduce the distillation temperature of the wash oil, a direct steam pipe is installed at the bottom of the regenerator, which introduces most or all of the steam required for benzene removal distillation.

　　在富油入口管下面舍两块弓形隔板，以提高再生器内洗油的蒸汽程度。在富油入口管的上面设三块形隔板，以捕集油滴。

　　Place two arched partitions under the rich oil inlet pipe to increase the steam level of the wash oil in the regenerator. Install three partition plates above the rich oil inlet pipe to capture oil droplets.

　　富油再生的油气和过热水蒸气从再生器顶部进入脱苯塔底部，作为富油脱苯蒸汽。该蒸汽中粗苯蒸汽分压与脱苯塔热贫油液面上粗苯蒸汽压接近，很难使脱苯贫油含苯量再进一步降低，贫油含苯质量含量一般在0.4%左右。

　　The oil and gas from the rich oil regeneration and the superheated steam enter the bottom of the benzene removal tower from the top of the regenerator as rich oil benzene removal steam. The partial pressure of crude benzene vapor in the steam is close to the pressure of crude benzene vapor on the hot lean oil surface of the benzene removal tower, making it difficult to further reduce the benzene content in the lean oil. The mass content of benzene in the lean oil is generally around 0.4%.

　　脱苯塔

　　Benzene removal tower

　　管式炉加热的泡罩脱苯塔，分两段，上段精馏段，下段提馏段。精馏段设有8块塔板，每块塔板上有若干个圆形泡罩，板间距为600mm。精馏段的第二层塔板及最下一层塔板为断塔板，以便将塔板上混有冷凝水的液体引至油水分离器，将水分离后再回到塔内下层塔板，以免塔内因冷凝水聚集而破坏精馏塔的正常操作。

　　The bubble hood dehalogenation tower heated by a tube furnace is divided into two sections: the upper distillation section and the lower distillation section. The distillation section is equipped with 8 trays, each with several circular bubble caps and a spacing of 600mm between them. The second and bottom trays of the distillation section are broken trays, which allow the liquid mixed with condensed water on the trays to be directed to the oil-water separator, separated, and then returned to the lower trays inside the tower to prevent the normal operation of the distillation tower from being disrupted by the accumulation of condensed water.

　　提馏段设有3块塔板，板间距为1000mm。每块塔板上有若干个圆形高泡罩及蛇管加热器，在塔板上保持较高的液面，使之能淹没加热器。重苯由提馏段底部排出。

　　The distillation section is equipped with three trays with a spacing of 1000mm. Each tray has several circular high bubble caps and coil heaters, which maintain a high liquid level on the tray to submerge the heaters. Heavy benzene is discharged from the bottom of the distillation section.

　　6、影响粗苯回收的主要因素

　　6. The main factors affecting the recovery of crude benzene

　　影响回收率的因素有煤气和洗油中粗苯含量、煤气流速及压力、洗油循环量及分子量、吸收操作温度、吸苯塔构造。

　　The factors that affect the recovery rate include the crude benzene content in gas and wash oil, gas flow rate and pressure, wash oil circulation and molecular weight, absorption operating temperature, and benzene absorption tower structure.

　　油库工段

　　Oil depot section

　　1、工艺说明

　　1. Process Description

　　本工段设置4个焦油贮槽（每个700m3， 存20天的焦油产量），接受冷凝鼓风装置送来的焦油，并装火车/汽车槽车外运；设置2个粗苯贮槽（每个400m3， 存20天的粗苯产量），接受粗苯蒸馏装置送来的粗苯，并装火车/汽车槽车外运；设置2个洗油贮槽（每个100m3， 存50天的用量），用于接受外来的洗油，并定期用泵送往终冷洗苯装置；设置2个（NaOH）碱贮槽（每台100m3， 存20天的用量）和2个硫酸槽（每个200m3），并用泵定期送至终冷洗苯装置和硫铵装置。当采用火车卸车时，利用火车卸车装置；当采用汽车装卸车时，利用汽车装卸车装置。

　　This section is equipped with four tar storage tanks (each 700m3, storing 20 days of tar production), which receive tar from the condensing blower device and transport it by train/truck tanker; Set up 2 crude benzene storage tanks (each 400m3, with a crude benzene production capacity of 20 days), receive crude benzene from the crude benzene distillation unit, and transport it by train/truck tank truck; Set up 2 wash oil storage tanks (each 100m3, with a storage capacity of 50 days) to receive external wash oil and regularly pump it to the final cold wash benzene unit; Set up 2 NaOH alkali storage tanks (100m3 each, with a storage capacity of 20 days) and 2 sulfuric acid tanks (200m3 each), and regularly pump them to the final cold washing benzene unit and ammonium sulfate unit. When using train unloading, utilize the train unloading device; When using car loading and unloading equipment, utilize the car loading and unloading device.

　　2、主要环保措施

　　2. Main environmental protection measures

　　1） 各贮槽放散气体经压力平衡系统回吸煤气管道，废气不外排。

　　1) The gas released from each storage tank is sucked back into the gas pipeline through the pressure balance system, and the exhaust gas is not discharged outside.

　　2） 焦油贮槽分离水送吸煤气管道，不外排。

　　2) The separated water from the tar storage tank is sent to the gas suction pipeline and is not discharged externally.

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