WO2020147607A1 - 一种焦炉煤气脱硫再生塔尾气处理工艺及系统 - Google Patents

一种焦炉煤气脱硫再生塔尾气处理工艺及系统 Download PDF

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WO2020147607A1
WO2020147607A1 PCT/CN2020/070523 CN2020070523W WO2020147607A1 WO 2020147607 A1 WO2020147607 A1 WO 2020147607A1 CN 2020070523 W CN2020070523 W CN 2020070523W WO 2020147607 A1 WO2020147607 A1 WO 2020147607A1
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gas
regeneration tower
liquid
mist
desulfurization regeneration
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PCT/CN2020/070523
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English (en)
French (fr)
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李昊阳
李超
赵国峰
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中冶焦耐(大连)工程技术有限公司
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Priority to JP2021536145A priority Critical patent/JP7174163B2/ja
Publication of WO2020147607A1 publication Critical patent/WO2020147607A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/52—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants

Definitions

  • the present disclosure relates to the technical field of coke oven gas purification, in particular to a coke oven gas desulfurization regeneration tower tail gas treatment process and system.
  • the removal of hydrogen sulfide from coke oven gas is an important process in the gas purification process.
  • the wet oxidation method is a common process used to remove hydrogen sulfide from raw gas. It has the advantages of low investment, high desulfurization efficiency, and low operating cost. At present, most domestic coking enterprises adopt this process.
  • the wet oxidation method When the wet oxidation method is used to remove hydrogen sulfide from raw gas, a large amount of air is passed into the bottom of the desulfurization regeneration tower to oxidize and regenerate the desulfurization rich liquid. After the excess air passes through the desulfurization regeneration tower, it becomes tail gas and is released at the top of the tower.
  • the specific process is as follows: After the desulfurization rich liquid and air are mixed, it enters the desulfurization regeneration tower from the bottom. While the rich liquid entering the desulfurization regeneration tower flows upward with a large amount of air, HS - is oxidized into elemental sulfur, and the desulfurization rich liquid is converted into desulfurization lean liquid .
  • the desulfurization lean liquid is produced at the desulfurization lean liquid outlet and sent to the desulfurization part for recycling.
  • the elemental sulfur generated by oxidation is bubbled by a large amount of air to form a sulfur foam.
  • the elemental sulfur overflows at the foamed sulfur outlet in the form of sulfur foam, and a large amount of air escapes from the gas phase outlet at the top of the desulfurization regeneration tower to become vent gas.
  • the tail gas released from the top of the desulfurization regeneration tower contains a certain amount of harmful gases such as hydrogen sulfide, hydrogen cyanide, ammonia, etc.
  • harmful gases such as hydrogen sulfide, hydrogen cyanide, ammonia, etc.
  • the tail gas of the desulfurization regeneration tower is not allowed to enter the atmosphere directly, and must be treated to achieve It can be released after emission standards.
  • the coke oven gas desulfurization system using wet oxidation process must add tail gas treatment facilities, which has caused a series of problems such as large area, high equipment investment and increased operating costs.
  • the present disclosure provides a coke oven gas desulfurization regeneration tower tail gas treatment process and system.
  • the oxidizing gas used for the oxidation and regeneration of the desulfurization rich liquid is cyclically used, so as to achieve no emission of gas in the system, and finally achieve no tail gas emission from the desulfurization regeneration tower the goal of.
  • a coke oven gas desulfurization regeneration tower tail gas treatment process includes the following steps:
  • the mist trapping layer is set on the top of the gas-liquid separator.
  • the mist trapped by the mist trapping layer is discharged from the liquid phase outlet at the bottom of the gas-liquid separator, and then returned to the desulfurization regeneration tower after being pressurized by the pump;
  • the separated gas phase is the circulating oxidizing gas. Escape from the gas phase outlet on the top of the gas-liquid separator and enter the gas pressurizing device;
  • the circulating oxidizing gas is pressurized by the gas pressurizing device, then mixed with supplementary oxidizing gas, and then mixed with the desulfurization rich liquid, and then enters the bottom of the desulfurization regeneration tower.
  • the circulating oxidizing gas is air or pure oxygen.
  • the supplemental oxidizing gas is pure oxygen.
  • the gas booster device is a fan, a gas booster pump or a gas booster valve.
  • step 2) a plurality of mist-catching layers are provided on the top of the gas-liquid separator, and the mist droplets captured by the plurality of mist-catching layers are discharged from the liquid phase outlet at the bottom of the gas-liquid separator. It is discharged and returned to the desulfurization regeneration tower after being pressurized by the pump.
  • the plurality of mist trapping layers are arranged in series.
  • the mist-catching layer is filled with fillers.
  • the coke oven gas desulfurization regeneration tower tail gas treatment process further includes washing the mist-catching layer with a washing medium.
  • the washing medium is water or liquid from the liquid phase outlet at the bottom of the gas-liquid separator.
  • the coke oven gas desulfurization regeneration tower tail gas treatment process further includes pressurizing the liquid from the liquid phase outlet at the bottom of the gas-liquid separator through a pump, and pressurizing the liquid from the bottom of the gas-liquid separator At least part of the liquid from the liquid phase outlet is delivered to the flushing nozzle above the mist-catching layer, and then the mist-catching layer is flushed through the flushing nozzle.
  • a coke oven gas desulfurization regeneration tower tail gas treatment system for realizing the process includes a desulfurization regeneration tower, a gas-liquid separator, a gas boosting device and a pump; the top of the desulfurization regeneration tower is provided with a gas phase outlet, The upper part of the desulfurization regeneration tower is provided with a desulfurization lean liquid outlet and a sulfur foam outlet; the middle of the desulfurization regeneration tower is provided with a separation liquid inlet, and the bottom of the desulfurization regeneration tower is provided with rich liquid and oxidizing gas inlets; the gas phase outlet of the desulfurization regeneration tower is connected with a gas-liquid separator The gas-liquid mixture inlet, the liquid-phase outlet at the bottom of the gas-liquid separator is connected to the inlet end of the pump, and the outlet end of the pump is connected to the separated liquid inlet of the desulfurization regeneration tower; the gas-phase outlet at the top of the gas-liquid separator is connected to the gas booster The inlet end is connected, the outlet end
  • one or more mist-catching layers are provided on the top of the gas-liquid separator, and the one or more mist-catching layers are configured to trap mist droplets.
  • a plurality of mist-catching layers are provided on the top of the gas-liquid separator, and the plurality of mist-catching layers are arranged in series.
  • the mist-catching layer is filled with fillers.
  • a flushing nozzle is arranged above the mist-catching layer, and the flushing nozzle is configured to use a flushing medium to flush the mist-catching layer.
  • the flushing nozzle is connected to the external flushing medium inlet through a pipeline.
  • the flushing nozzle is connected to the outlet of the pump at the liquid phase outlet at the bottom of the gas-liquid separator through a pipeline, so that at least part of the liquid phase outlet from the bottom of the gas-liquid separator The liquid is delivered to the washing nozzle as a washing medium.
  • the washing medium is water.
  • Figure 1 is a schematic structural diagram of a coke oven gas desulfurization regeneration tower tail gas treatment system described in the present disclosure.
  • Fig. 2 is a schematic structural diagram of the coke oven gas desulfurization regeneration tower tail gas treatment system shown in Fig. 1 of the present disclosure with a flushing system for flushing the mist-catching layer.
  • the process for treating tail gas from a coke oven gas desulfurization regeneration tower described in the present disclosure includes the following steps:
  • a mist-catching layer 10 is set on the top of the gas-liquid separator 8.
  • the mist trapped by the mist-catching layer 10 is discharged from the liquid phase outlet at the bottom of the gas-liquid separator 10, pressurized by the pump 11 and returned to the desulfurization regeneration tower 1; the separated gas phase For circulating oxidizing gas, it escapes from the gas phase outlet at the top of the gas-liquid separator 8 and enters the gas pressurizing device 9;
  • the circulating oxidizing gas is pressurized by the gas pressurizing device 9 first, then mixed with the supplementary oxidizing gas, and then mixed with the desulfurization rich liquid, and then enters the bottom of the desulfurization regeneration tower 1.
  • the circulating oxidizing gas is air or pure oxygen.
  • the supplemental oxidizing gas is pure oxygen.
  • the gas boosting device 9 is a fan, a gas boosting pump or a gas boosting valve.
  • step 2) the top 15 of the gas-liquid separator is provided with a plurality of mist-catching layers, and the mist droplets captured by the plurality of mist-catching layers are separated from the liquid phase at the bottom of the gas-liquid separator.
  • the outlet is discharged and returned to the desulfurization regeneration tower after being pressurized by the pump.
  • the plurality of mist trapping layers are arranged in series.
  • the mist-catching layer is filled with fillers.
  • the coke oven gas desulfurization regeneration tower tail gas treatment process further includes washing the mist-catching layer with a washing medium.
  • the washing medium is water or liquid from the liquid phase outlet at the bottom of the gas-liquid separator.
  • the coke oven gas desulfurization regeneration tower tail gas treatment process further includes pressurizing the liquid from the liquid phase outlet at the bottom of the gas-liquid separator through the pump 11, and pressurizing the liquid from the gas-liquid separator At least part of the liquid from the liquid phase outlet at the bottom is delivered to the washing nozzle 16 above the mist-catching layer, and then the mist-catching layer is washed by the washing nozzle 16.
  • the flushing step may be performed simultaneously with the exhaust gas treatment process, or may be performed during the shutdown of the exhaust gas treatment process.
  • the flushing of the mist-trapping layer solves the problem of excessive resistance of the flow (especially gas) through the mist-trapping layer caused by the blockage of the mist-trapping layer by the solid or viscous liquid in the exhaust gas to be processed. This helps to increase the throughput of the exhaust gas and improve the efficiency of the overall process.
  • the present disclosure uses the liquid from the liquid phase outlet at the bottom of the gas-liquid separator as the washing medium to realize the recycling of materials, reduce the operating cost, and simplify the washing process.
  • the second valve 18 and the first valve 17 can be controlled as needed to select whether to use the external flushing medium from the external flushing medium inlet 14 or to use the liquid from the liquid phase outlet 13 at the bottom of the gas-liquid separator to perform the mist trapping layer. rinse.
  • the mist trap layer also called mist trap, is used to separate the mist entrained in the gas, reduce the loss of valuable materials and/or remove undesirable impurities or pollutants from the gas, such as hydrogen sulfide and hydrogen cyanide And ammonia.
  • the mist trapping layer removes the mist droplets that may contain hydrogen sulfide, hydrogen cyanide and ammonia in the exhaust gas emitted at the top of the desulfurization regeneration tower, thereby obtaining exhaust gas that can be discharged into the atmosphere.
  • the mist-trapping layer can effectively remove 3-5 ⁇ m mist droplets.
  • the mist-catching layer can have various structures.
  • the mist-catching layer can be composed of a plate and a supporting device.
  • the plates of the mist-catching layer are usually made of polymer materials (such as polypropylene, FRP, etc.) or stainless steel (such as 316L, 317L, etc.) materials.
  • the plate can be a corrugated plate or a zigzag plate configured to form a tortuous channel.
  • the general working principle of this kind of mist-catching layer is: when the gas containing mist droplets flows through the mist-catching layer at a certain speed, due to the inertial impact of the gas, the mist droplets collide with the corrugated plate and are gathered into droplets; When the size of the droplet is so large that its own gravity exceeds the combined force of the rising force of the gas and the surface tension of the liquid, the droplet is separated from the surface of the corrugated plate.
  • the multi-folding structure of the corrugated plate of the mist-catching layer increases the chance of mist being trapped. The mist that has not been removed will be trapped by the same action at the next turning. This repeated action will greatly improve the efficiency of mist removal. . After the gas passes through the corrugated plate demister, there is basically no mist.
  • the flow rate of the gas containing mist droplets through the mist-trapping layer is, for example, 3.5-5.5 m/s.
  • the mist-catching layer is also provided in other structures as long as it can make the mist droplets collide with the plate.
  • the mist-catching layer may also be filled with fillers.
  • the filler of the mist-trapping layer can further prevent the mist from being discharged from the top of the gas-liquid separator with the gas.
  • step 1) the desulfurization absorbing hydrogen sulfide gas shortage rich liquid containing suspended sulfur, S 2 O 3 2-, HS -, CNS -, CN - and other substances.
  • the desulfurization rich liquid if ammonia desulfurization is used in the desulfurization regeneration tower, the desulfurization rich liquid also contains free ammonia and NH 4 + .
  • the desulfurization rich liquid if alkali desulfurization is used in the desulfurization regeneration tower, the desulfurization rich liquid also contains Na + , CO 3 2- , and HCO 3 ⁇ .
  • the desulfurization rich liquid enters the desulfurization regeneration tower to be oxidized and regenerated, and HS - is oxidized to generate elemental sulfur, which overflows from the top of the tower in the form of sulfur foam.
  • the operating pressure of the desulfurization regeneration tower is 0-10Kpag, and the operating temperature is 28-45°C.
  • a large amount of oxidizing gas escapes from the gas phase outlet at the top of the desulfurization regeneration tower and enters the gas-liquid separator.
  • the operating pressure of the gas-liquid separator is 0-10Kpag.
  • the oxidizing gas entering the gas-liquid separator 8 is mainly composed of nitrogen, oxygen, and a small amount of hydrogen sulfide and ammonia.
  • the oxidizing gas also contains a certain amount of carbon dioxide.
  • step 2) a mist-catching layer is set on the top of the gas-liquid separator, and the mist captured by the mist-catching layer is discharged from the liquid phase outlet at the bottom of the gas-liquid separator, pressurized by a pump to 20 ⁇ 200Kpag (for example, 20 ⁇ 60Kpag) and then returned Desulfurization regeneration tower; the separated gas phase is a circulating oxidizing gas, which escapes from the gas phase outlet at the top of the gas-liquid separator and enters the gas pressurizing device.
  • 20 ⁇ 200Kpag for example, 20 ⁇ 60Kpag
  • step 3 the circulating oxidizing gas is first pressurized to 500-800 kpag by a gas pressurizing device, mixed with supplementary oxidizing gas, and then mixed with the desulfurization rich liquid, and then enters the bottom of the desulfurization regeneration tower.
  • a coke oven gas desulfurization regeneration tower tail gas treatment system for realizing the process includes a desulfurization regeneration tower 1, a gas-liquid separator 8, a gas booster 9 and a pump 11; the tower of the desulfurization regeneration tower 1 The top of the gas phase outlet is provided, the upper part of the desulfurization regeneration tower 1 is provided with a desulfurization lean liquid outlet 4 and a sulfur foam outlet 5; the middle of the desulfurization regeneration tower 1 is provided with a separation liquid inlet 12, and the bottom of the desulfurization regeneration tower 1 is provided with rich liquid and oxidizing gas inlets;
  • the gas phase outlet of the desulfurization regeneration tower 1 is connected to the gas-liquid mixture inlet of the gas-liquid separator 8, the liquid phase outlet at the bottom of the gas-liquid separator 8 is connected to the inlet end of the pump 11, and the outlet end of the pump 11 is connected to the separation liquid of the desulfurization regeneration tower 1.
  • the inlet 12 is connected; the gas-phase outlet on the top of the gas-liquid separator 8 is connected to the inlet end of the gas boosting device 9, and the outlet end of the gas boosting device 9 is connected to the mixing pipe 6 through the circulating gas pipe 3, and the circulating gas pipe 3 is provided with supplementary oxidation
  • the mixing pipe 6 is also provided with a desulfurization rich liquid inlet 2, and the outlet of the mixing pipe 6 is connected to the rich liquid and oxidizing gas inlet at the bottom of the desulfurization regeneration tower 1.
  • the gas phase at the top of the desulfurization regeneration tower 1 is separated and demisted by the gas-liquid separator 8, and then pressurized by the gas pressurizing device 9, and then mixed with the supplementary oxidizing gas and then re-entered into the desulfurization regeneration tower 1 for recycling.
  • the system realizes closed-loop operation, thus achieving the goal of no exhaust emissions.
  • one or more mist trapping layers are provided on the top of the gas-liquid separator, and the one or more mist trapping layers are configured to trap mist droplets.
  • a plurality of mist-catching layers are provided on the top of the gas-liquid separator, and the plurality of mist-catching layers are arranged in series.
  • the mist-catching layer is filled with fillers.
  • a flushing nozzle is arranged above the mist-catching layer, and the flushing nozzle is configured to use a flushing medium to flush the mist-catching layer.
  • the flushing medium is an external flushing medium
  • the external flushing medium inlet is connected to the flushing nozzle through a pipe.
  • the flushing nozzle is connected to the outlet of the pump at the liquid phase outlet at the bottom of the gas-liquid separator through a pipeline, so that at least part of the liquid phase outlet from the bottom of the gas-liquid separator The liquid is delivered to the washing nozzle as a washing medium.
  • the flushing nozzle is connected to both the outlet of the pump at the liquid phase outlet at the bottom of the gas-liquid separator and the inlet of the external flushing medium.
  • the system further includes a valve provided between the flushing nozzle and the outlet of the pump at the liquid phase outlet at the bottom of the gas-liquid separator, and the flushing nozzle and the external The valve between the flushing medium inlet.
  • the flushing nozzle is simultaneously connected with the pump at the liquid phase outlet at the bottom of the gas-liquid separator and the external flushing medium inlet.
  • a valve is provided between the flushing nozzle and the pump at the liquid phase outlet at the bottom of the gas-liquid separator.
  • a valve is provided between the flushing nozzle and the external flushing medium inlet.
  • the oxidizing gas used for the oxidation and regeneration of the desulfurization rich liquid is recycled, so as to realize the system without emission of gas, and finally achieve the goal of no tail gas emission from the desulfurization regeneration tower.
  • the conventional tail gas treatment process it has the advantages of less additional area, convenient operation, less investment and low operating cost.

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Abstract

一种焦炉煤气脱硫再生塔（1）尾气处理工艺及系统，脱硫再生塔（1）内脱硫富液被氧化再生后，大量氧化性气体从塔顶气相出口逸出进入气液分离器（8）；气液分离器（8）顶部设置捕雾层（10），捕雾层（10）捕获的雾滴由气液分离器（8）底部液相出口排出，经泵（11）增压后返回脱硫再生塔（1）；分离出的气相为循环氧化性气体，由气液分离器（8）顶部气相出口逸出，进入气体增压装置（9）；循环氧化性气体先经气体增压装置（9）增压，然后与补充氧化性气体混合，再与脱硫富液混合后进入脱硫再生塔（1）底部。将用于脱硫富液氧化再生的氧化性气体进行循环使用，从而实现系统无放散气体产生，最终达到脱硫再生塔无尾气排放的目的。

Description

一种焦炉煤气脱硫再生塔尾气处理工艺及系统
相关申请的交叉引用
本申请要求于2019年1月17日提交中国专利局的申请号为201910042637.X、名称为“一种焦炉煤气脱硫再生塔尾气处理工艺及系统”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本公开涉及焦炉煤气净化技术领域，尤其涉及一种焦炉煤气脱硫再生塔尾气处理工艺及系统。
背景技术
焦炉煤气脱除硫化氢是煤气净化工艺的重要工序。湿式氧化法是一种用于脱除荒煤气中硫化氢的常见工艺，具有投资省、脱硫效率高、操作费用低等优点，目前国内焦化企业大多采用该工艺。
采用湿式氧化法脱除荒煤气中硫化氢时，在脱硫再生塔塔底通入大量空气对脱硫富液进行氧化再生后，过量的空气经过脱硫再生塔后成为尾气在塔顶放散。具体过程为：脱硫富液和空气混合后，从底部进入脱硫再生塔，进入脱硫再生塔的富液与大量空气向上流动的同时，HS -被氧化成为单质硫，脱硫富液转化为脱硫贫液。脱硫贫液在脱硫贫液出口被采出送至脱硫部分循环使用。氧化生成的单质硫被大量的空气通过鼓泡形成硫泡沫，单质硫以硫泡沫形式在泡沫硫出口溢出，大量空气从脱硫再生塔塔顶的气相出口逸出成为放散气。
脱硫再生塔塔顶放散的尾气中含有一定量的硫化氢、氰化氢、氨等有害气体，随着国家对环保要求的日益严格，脱硫再生塔的尾气不允许直接进入大气，必须经过处理达到排放标准之后才可以放散。目前采用湿式氧化法工艺的焦炉煤气脱硫系统必须增加尾气处理设施，从而产生了占地面积大、装置投资高以及运行费用增加等一系列问题。
发明内容
本公开提供了一种焦炉煤气脱硫再生塔尾气处理工艺及系统，将用于脱硫富液氧化再生的氧化性气体进行循环使用，从而实现系统无放散气体产生，最终达到脱硫再生塔无尾气排放的目的。
为了达到上述目的，本公开采用以下技术方案实现：
一种焦炉煤气脱硫再生塔尾气处理工艺，包括如下步骤：
1)脱硫再生塔内脱硫富液被氧化再生后，大量氧化性气体从塔顶气相出口逸出，进入气液分离器；
2)气液分离器顶部设置捕雾层，捕雾层捕获的雾滴由气液分离器底部液相出口排出，经泵增压后返回脱硫再生塔；分离出的气相为循环氧化性气体，由气液分离器顶部气相出口逸出，进入气体增压装置；
3)循环氧化性气体先经气体增压装置增压，然后与补充氧化性气体混合，再与脱硫富液混合后进入脱硫再生塔底部。
在一种或多种实施方式中，所述循环氧化性气体为空气或纯氧气。
在一种或多种实施方式中，所述补充氧化性气体为纯氧气。
在一种或多种实施方式中，所述气体增压装置为风机、气体增压泵或气体增压阀。
在一种或多种实施方式中，在步骤2)中，所述气液分离器顶部设置多个捕雾层，所述多个捕雾层捕获的雾滴由气液分离器底部液相出口排出，经泵增压后返回脱硫再生塔。
在一种或多种实施方式中，所述多个捕雾层以串联的方式布置。
在一种或多种实施方式中，所述捕雾层中填充有填料。
在一种或多种实施方式中，所述焦炉煤气脱硫再生塔尾气处理工艺还包括使用冲洗介质冲洗所述捕雾层。
在一种或多种实施方式中，所述冲洗介质为水或来自气液分离器底部液相出口的液体。
在一种或多种实施方式中，所述焦炉煤气脱硫再生塔尾气处理工艺还包括通过泵增压来自气液分离器底部液相出口的液体，并将增压的来自气液分离器底部液相出口的至少部分液体输送至所述捕雾层上方的冲洗喷头，然后通过所述冲洗喷头冲洗捕雾层。
一种用于实现所述工艺的一种焦炉煤气脱硫再生塔尾气处理系统，包括脱硫再生塔、气液分离器、气体增压装置及泵；所述脱硫再生塔的塔顶设气相出口，脱硫再生塔的上部设脱硫贫液出口及硫泡沫出口；脱硫再生塔的中部设分离液入口，脱硫再生塔的底部设富液及氧化性气体入口；脱硫再生塔的气相出口连接气液分离器的气液混合物入口，气液分离器底部的液相出口与泵的入口端相连，泵的出口端与脱硫再生塔的分离液入口相连；气液分离器顶部的气相出口与气体增压装置的入口端相连，气体增压装置的出口端通过循环气体管道连接混合管道，循环气体管道上设补充氧化性气体入口；混合管道上还设有脱硫富液入口，混合管道的出口连接脱硫再生塔底部的富液及氧化性气体入口。
在一种或多种实施方式中，所述气液分离器顶部设置一个或多个捕雾层，所述一个 或多个捕雾层被配置为捕获雾滴。
在一种或多种实施方式中，所述气液分离器顶部设置多个捕雾层，所述多个捕雾层以串联的方式布置。
在一种或多种实施方式中，所述捕雾层填充有填料。
在一种或多种实施方式中，所述捕雾层上方设置有冲洗喷头，所述冲洗喷头被配置为使用冲洗介质来冲洗所述捕雾层。
在一种或多种实施方式中，所述冲洗喷头通过管路与外部冲洗介质入口相连。
在一种或多种实施方式中，所述冲洗喷头通过管路与气液分离器底部的液相出口处的所述泵的出口相连，使得来自气液分离器底部的液相出口的至少部分液体作为冲洗介质被输送至所述冲洗喷头。
在一种或多种实施方式中，所述冲洗介质为水。
本公开的有益效果至少包括：
1)将用于脱硫富液氧化再生的氧化性气体进行循环使用，从而实现系统无放散气体产生，最终达到脱硫再生塔无尾气排放的目的；
2)与常规尾气处理工艺相比，具有额外增加的占地少，操作方便，且投资少、运行费用低的优点。
附图说明
为了更清楚地说明本公开实施方式的技术方案，下面将对实施方式中所需要使用的附图作简单地介绍，应当理解，以下附图仅示出了本公开的某些实施方式，因此不应被看作是对范围的限定，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他相关的附图。
图1是本公开所述一种焦炉煤气脱硫再生塔尾气处理系统的结构示意图。
图2是本公开图1所示的焦炉煤气脱硫再生塔尾气处理系统的基础上增加了用于冲洗捕雾层的冲洗系统的结构示意图。
图中：1.脱硫再生塔
2.脱硫富液入口
3.循环气体管道
4.脱硫贫液出口
5.硫泡沫出口
6.混合管道
7.补充氧化性气体入口
8.气液分离器
9.气体增压装置
10.捕雾层
11.泵
12.分离液入口。
13.气液分离器底部液相出口
14.外部冲洗介质入口
15.气液分离器顶部
16.冲洗喷头
17.第一阀
18.第二阀
具体实施方式
为使本公开实施方式的目的、技术方案和优点更加清楚，下面将对本公开实施方式中的技术方案进行清楚、完整地描述。实施方式中未注明具体条件者，按照常规条件或制造商建议的条件进行。所用试剂或仪器未注明生产厂商者，均为可以通过市售购买获得的常规产品。
除非本文另有定义，否则结合本公开使用的科学和技术术语应具有本领域普通技术人员通常理解的含义。以下描述示例性方法和材料，但是与本文描述的那些类似或等同的方法和材料也可以用于本公开的实践或测试中。
下面结合附图对本公开的具体实施方式作进一步说明：
如图1所示，本公开所述一种焦炉煤气脱硫再生塔尾气处理工艺，包括如下步骤：
1)脱硫再生塔1内脱硫富液被氧化再生后，大量氧化性气体从塔顶气相出口逸出，进入气液分离器8；
2)气液分离器8顶部设置捕雾层10，捕雾层10捕获的雾滴由气液分离器10底部液相出口排出，经泵11增压后返回脱硫再生塔1；分离出的气相为循环氧化性气体，由气液分离器8顶部气相出口逸出，进入气体增压装置9；
3)循环氧化性气体先经气体增压装置9增压，然后与补充氧化性气体混合，再与脱硫富液混合后进入脱硫再生塔1底部。
在一种或多种实施方式中，所述循环氧化性气体为空气或纯氧气。
在一种或多种实施方式中，所述补充氧化性气体为纯氧气。
在一种或多种实施方式中，所述气体增压装置9为风机、气体增压泵或气体增压阀。
在一种或多种实施方式中，在步骤2)中，所述气液分离器顶部15设置多个捕雾层，所述多个捕雾层捕获的雾滴由气液分离器底部液相出口排出，经泵增压后返回脱硫再生塔。
在一种或多种实施方式中，所述多个捕雾层以串联的方式布置。
在一种或多种实施方式中，所述捕雾层中填充有填料。
在一种或多种实施方式中，所述焦炉煤气脱硫再生塔尾气处理工艺还包括使用冲洗介质冲洗所述捕雾层。
在一种或多种实施方式中，所述冲洗介质为水或来自气液分离器底部液相出口的液体。
在一种或多种实施方式中，所述焦炉煤气脱硫再生塔尾气处理工艺还包括通过泵11增压来自气液分离器底部液相出口的液体，并将增压的来自气液分离器底部液相出口的至少部分液体输送至所述捕雾层上方的冲洗喷头16，然后通过所述冲洗喷头16冲洗捕雾层。
冲洗步骤可以随尾气处理工艺同时进行，也可以在尾气处理工艺的停车期间进行。对捕雾层的冲洗解决了可能由于待处理尾气中的固体或粘稠液体对捕雾层的堵塞造成的物流(特别是气体)通过捕雾层的阻力过大的问题。这有助于提高对尾气的处理通量，提高整体工艺的效率。
特别地，在一种或多种实施方式中，本公开使用来自气液分离器底部液相出口的液体作为冲洗介质，实现了物料的循环利用，减少了操作成本，简化了冲洗工艺。
本公开的上述工艺的各个步骤或特点可以根据需要相互组合，这并不超出本公开要求保护范围。
例如，可以根据需要通过控制第二阀18以及第一阀17来选择是使用来自外部冲洗介质入口14的外部冲洗介质还是使用来自气液分离器底部液相出口13的液体来对捕雾层进行冲洗。
捕雾层，也可称作捕雾器，用于分离气体中夹带的雾滴，降低有价值的物料损失和/或从气体中除去不希望的杂质或污染物，例如硫化氢、氰化氢和氨。例如在本文中，通过捕雾层除去掺杂在脱硫再生塔塔顶放散的尾气中的可能包含硫化氢、氰化氢和氨的雾滴，从而得到可以排放到大气中的尾气。
在一种或多种实施方式中，捕雾层可以有效除去3-5μm的雾滴。
捕雾层可以具有各种结构。例如，捕雾层可以由板片和支承装置构成。
在一种或多种实施方式中，捕雾层的板片通常由高分子材料(如聚丙稀PP、FRP等)或不锈钢(如316L、317L等)类材料制作而成。
在一种或多种实施方式中，板片可以是配置成形成曲折通道的波形板或折线形板。这种捕雾层的一般的工作原理为：当含有雾滴的气体以一定速度流经捕雾层时，由于气体的惯性撞击作用，雾滴与波形板片相碰撞而被聚成液滴；当液滴的尺寸大到其自身产生的重力超过气体的上升力与液体表面张力的合力时，液滴就从波形板表面上被分离下来。捕雾层波形板的多折向结构增加了雾滴被捕集的机会，未被除去的雾滴在下一个转弯处经过相同的作用而被捕集，这样反复作用，从而大大提高了除雾效率。气体通过波形板除雾器后，基本上不含雾滴。
在一种或多种实施方式中，含有雾滴的气体通过捕雾层的流速为例如3.5-5.5m/s。
捕雾层也设置为其他结构，只要其可以使得雾滴与板片碰撞即可。
在一种或多种实施方式中，捕雾层也可以填充有填料。捕雾层的填料可以进一步阻止雾滴随气体从气液分离器的顶部排出。
在步骤1)中，吸收了荒煤气中硫化氢的脱硫富液，含有悬浮硫、S 2O 3 2-、HS -、CNS -、CN -等物质。在一种或多种实施方式，如果脱硫再生塔内采用氨法脱硫，则脱硫富液还含有游离氨和NH 4 +。在一种或多种实施方式，如果脱硫再生塔内采用碱法脱硫，则脱硫富液还含有Na +、CO 3 2-、HCO3 -。脱硫富液进入脱硫再生塔被氧化再生，HS -被氧化生成单质硫，从塔顶以硫泡沫的形式溢出。在一种或多种实施方式中，脱硫再生塔操作压力为0～10Kpag，操作温度为28～45℃。大量氧化性气体从脱硫再生塔塔顶气相出口逸出，进入气液分离器。在一种或多种实施方式中，气液分离器操作压力为0～10Kpag。在一种或多种实施方式中，进入气液分离器8的氧化性气体主要由氮气、氧气以及少量的硫化氢和氨气组成。在脱硫再生塔内采用碱法脱硫的情况下，氧化性气体还含有一定量二氧化碳。
在步骤2)中，气液分离器顶部设置捕雾层，捕雾层捕获的雾滴由气液分离器底部液相出口排出，经泵增压至20～200Kpag(例如20～60Kpag)后返回脱硫再生塔；分离出的气相为循环氧化性气体，由气液分离器顶部气相出口逸出，进入气体增压装置。
在步骤3)中，循环氧化性气体先经气体增压装置增压至500～800kpag后，与补充氧化性气体混合，再与脱硫富液混合后进入脱硫再生塔底部。
一种用于实现所述工艺的一种焦炉煤气脱硫再生塔尾气处理系统，包括脱硫再生塔1、气液分离器8、气体增压装置9及泵11；所述脱硫再生塔1的塔顶设气相出口，脱硫再生塔1的上部设脱硫贫液出口4及硫泡沫出口5；脱硫再生塔1的中部设分离液入口12，脱硫再生塔1的底部设富液及氧化性气体入口；脱硫再生塔1的气相出口连接气液分离器8的气液混合物入口，气液分离器8底部的液相出口与泵11的入口端相连，泵11的出口端与脱硫再生塔1的分离液入口12相连；气液分离器8顶部的气相出口与气体增压装置9的入口端相连，气体增压装置9的出口端通过循环气体管道3连接混合管道6，循环气体管 道3上设补充氧化性气体入口；混合管道6上还设有脱硫富液入口2，混合管道6的出口连接脱硫再生塔1底部的富液及氧化性气体入口。
本公开中，脱硫再生塔1塔顶的气相经气液分离器8分离除雾后，再经气体增压装置9增压，然后与补充氧化性气体混合后重新进入脱硫再生塔1循环利用，系统实现闭环运行，由此实现无尾气排放的目的。
在一种或多种实施方式中，所述气液分离器顶部设置一个或多个捕雾层，所述一个或多个捕雾层被配置为捕获雾滴。
在一种或多种实施方式中，所述气液分离器顶部设置多个捕雾层，所述多个捕雾层以串联的方式布置。
在一种或多种实施方式中，所述捕雾层填充有填料。
在一种或多种实施方式中，所述捕雾层上方设置有冲洗喷头，所述冲洗喷头被配置为使用冲洗介质来冲洗所述捕雾层。
在一种或多种实施方式中，所述冲洗介质为外部冲洗介质，所述外部冲洗介质入口通过管道与所述冲洗喷头相连。
在一种或多种实施方式中，所述冲洗喷头通过管路与气液分离器底部的液相出口处的所述泵的出口相连，使得来自气液分离器底部的液相出口的至少部分液体作为冲洗介质被输送至所述冲洗喷头。
在一种或多种实施方式中，所述冲洗喷头与气液分离器底部的液相出口处的所述泵的出口以及外部冲洗介质入口二者相连。
在一种或多种实施方式中，所述系统还包括设置在所述冲洗喷头与气液分离器底部的液相出口处的所述泵的出口之间的阀门，以及所述冲洗喷头与外部冲洗介质入口之间的阀门。
本文所述的系统可用于实现上述焦炉煤气脱硫再生塔尾气处理工艺
在一种或多种实施方式中，冲洗喷头同时与气液分离器底部的液相出口处的泵以及外部冲洗介质入口相连。在一种或多种实施方式中，在冲洗喷头与气液分离器底部的液相出口处的泵之间设置有阀门。在一种或多种实施方式中，在冲洗喷头与外部冲洗介质入口之间设置有阀门。这样的设计便于根据具体情况，选择合适的冲洗介质。例如气液分离器底部的液相出口的液体杂质过多或过于粘稠不适合冲洗捕雾层的情况下，可以使用外部的冲洗介质，例如水，来冲洗捕雾层。
以上所述，仅为本公开较佳的具体实施方式，但本公开的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本公开揭露的技术范围内，根据本公开的技术方案及其公开构思加以等同替换或改变，都应涵盖在本公开的保护范围之内。
工业实用性
将用于脱硫富液氧化再生的氧化性气体进行循环使用，从而实现系统无放散气体产生，最终达到脱硫再生塔无尾气排放的目的。与常规尾气处理工艺相比，具有额外增加的占地少，操作方便，且投资少、运行费用低的优点。

Claims (19)

  1. 一种焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，包括如下步骤：
    1)脱硫再生塔内脱硫富液被氧化再生后，大量氧化性气体从塔顶气相出口逸出，进入气液分离器；
    2)气液分离器顶部设置捕雾层，捕雾层捕获的雾滴由气液分离器底部液相出口排出，经泵增压后返回脱硫再生塔；分离出的气相为循环氧化性气体，由气液分离器顶部气相出口逸出，进入气体增压装置；
    3)循环氧化性气体先经气体增压装置增压，然后与补充氧化性气体混合，再与脱硫富液混合后进入脱硫再生塔底部。
  2. 根据权利要求1所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，所述循环氧化性气体为空气或纯氧气。
  3. 根据权利要求1或2所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，所述补充氧化性气体为纯氧气。
  4. 根据权利要求1-3中任一项所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，所述气体增压装置为风机、气体增压泵或气体增压阀。
  5. 根据权利要求1-4中任一项所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，在步骤2)中，所述气液分离器顶部设置多个捕雾层，所述多个捕雾层捕获的雾滴由气液分离器底部液相出口排出，经泵增压后返回脱硫再生塔。
  6. 根据权利要求5所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，所述多个捕雾层以串联的方式布置。
  7. 根据权利要求1-6中任一项所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，所述捕雾层中填充有填料。
  8. 根据权利要求1-7中任一项所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，所述焦炉煤气脱硫再生塔尾气处理工艺还包括使用冲洗介质冲洗所述捕雾层。
  9. 根据权利要求8所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，所述冲洗介质为水或来自气液分离器底部液相出口的液体。
  10. 根据权利要求8所述的焦炉煤气脱硫再生塔尾气处理工艺，其特征在于，所述焦炉煤气脱硫再生塔尾气处理工艺还包括通过所述泵增压来自气液分离器底部液相出口的液体，并将增压的来自气液分离器底部液相出口的至少部分液体输送至所述捕雾层上方的冲洗喷头，然后通过所述冲洗喷头冲洗捕雾层。
  11. 一种用于实现权利要求1所述工艺的一种焦炉煤气脱硫再生塔尾气处理系统， 其特征在于，所述系统包括脱硫再生塔、气液分离器、气体增压装置及泵；
    所述脱硫再生塔的塔顶设气相出口，所述脱硫再生塔的上部设脱硫贫液出口及硫泡沫出口；
    所述脱硫再生塔的中部设分离液入口，所述脱硫再生塔的底部设富液及氧化性气体入口；
    所述脱硫再生塔的气相出口连接所述气液分离器的气液混合物入口，所述气液分离器底部的液相出口与所述泵的入口端相连，所述泵的出口端与所述脱硫再生塔的分离液入口相连；
    所述气液分离器顶部的气相出口与所述气体增压装置的入口端相连，所述气体增压装置的出口端通过循环气体管道连接混合管道，所述循环气体管道上设补充氧化性气体入口；
    所述混合管道上还设有脱硫富液入口，所述混合管道的出口连接所述脱硫再生塔底部的富液及氧化性气体入口。
  12. 根据权利要求11所述的系统，其特征在于，所述气液分离器顶部设置一个或多个捕雾层，所述一个或多个捕雾层被配置为捕获雾滴。
  13. 根据权利要求11所述的系统，其特征在于，所述气液分离器顶部设置多个捕雾层，所述多个捕雾层以串联的方式布置。
  14. 根据权利要求12或13所述的系统，其特征在于，所述捕雾层填充有填料。
  15. 根据权利要求11-14中任一项所述的系统，其特征在于，所述捕雾层上方设置有冲洗喷头，所述冲洗喷头被配置为使用冲洗介质来冲洗所述捕雾层。
  16. 根据权利要求15所述的系统，其特征在于，所述冲洗介质为来自外部的冲洗介质，所述来自外部的冲洗介质的入口通过管道与所述冲洗喷头相连。
  17. 根据权利要求15所述的系统，其特征在于，所述冲洗喷头通过管路与气液分离器底部的液相出口处的所述泵的出口相连，使得来自气液分离器底部的液相出口的至少部分液体作为冲洗介质被输送至所述冲洗喷头。
  18. 根据权利要求15所述的系统，其特征在于，所述冲洗喷头与气液分离器底部的液相出口处的所述泵的出口以及外部冲洗介质入口二者相连。
  19. 根据权利要求18所述的系统，其特征在于，所述系统还包括设置在所述冲洗喷头与气液分离器底部的液相出口处的所述泵的出口之间的阀门，以及所述冲洗喷头与外部冲洗介质入口之间的阀门。
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