WO2022179112A1 - 一种裂解油气多级冷却净化装置 - Google Patents

一种裂解油气多级冷却净化装置 Download PDF

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WO2022179112A1
WO2022179112A1 PCT/CN2021/122997 CN2021122997W WO2022179112A1 WO 2022179112 A1 WO2022179112 A1 WO 2022179112A1 CN 2021122997 W CN2021122997 W CN 2021122997W WO 2022179112 A1 WO2022179112 A1 WO 2022179112A1
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oil
gas
tower
cooling
inlet
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PCT/CN2021/122997
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English (en)
French (fr)
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赵凤娇
刘萍
张广震
吴元旭
王大龙
牛斌
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济南恒誉环保科技股份有限公司
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Priority to ZA2021/09509A priority Critical patent/ZA202109509B/en
Publication of WO2022179112A1 publication Critical patent/WO2022179112A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
    • B01D5/0012—Vertical tubes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

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  • the invention belongs to the technical field of waste cracking, and in particular relates to a multi-stage cooling and purification device for cracked oil and gas.
  • the present invention proposes a multi-stage cooling and purification device for cracked oil and gas.
  • the device includes a first cooler and a second cooler arranged in series.
  • the two coolers have the same structure and both include a horizontally arranged oil storage tank.
  • a multi-stage cooling and purifying device for cracked oil and gas includes a first cooler and a second cooler arranged in series, the two coolers have the same structure, and both include a horizontally arranged oil storage tank, and an oil and gas inlet is connected to the oil storage tank.
  • Tower and oil and gas condensing tower The oil and gas condensing tower is provided with a condensing pipeline, and a cooling cavity is set on the outside of the condensing pipeline.
  • the cooling cavity is connected with a cooling medium inlet and a cooling medium outlet. After the oil and gas enters the oil and gas condensing tower, it goes up the condensing pipeline sports;
  • the flue gas purification system and the regenerative circulating fan are directly connected through a pipeline, and the pipeline is provided with a control valve;
  • the temperature is constant within the specified temperature range;
  • the high-temperature oil vapor generated from the cracker enters the first oil and gas inlet tower through the first oil and gas inlet, and fills the tower body and finally presses down into the first oil storage tank and the oil storage tank
  • the pre-installed oil is contacted, and the solid components are eluted through it. Since the oil in the oil storage tank is not fully loaded, a cavity is left in the top of the first oil storage tank to facilitate the movement of oil and gas.
  • the removed oil and gas enters the first oil and gas condensing tower;
  • the high-temperature flue gas as the heat source of the cracker enters the flue gas inlet pipe through the regenerative circulating fan, and at the same time, the low-temperature air is brought in through the air inlet pipe to reduce the temperature of the flue gas and then enter the first oil and gas condensing tower;
  • the ratio of low temperature air to high temperature flue gas is controlled to realize the control of the first oil and gas outlet temperature of the first condensing tower, generally
  • the outlet temperature is controlled to be greater than 360°C.
  • the reason for this design is to keep the oil that can be converted into liquid within this temperature range in the first oil storage tank. This part of the oil is mentioned in the background art.
  • this part of the oil and solid components are regularly discharged into the cracker through the circulating pump; this time is generally controlled within 4 -5 hours is a cycle, which can also be adjusted according to specific working conditions.
  • the oil and solid components returned to the cracker can be processed together with the newly added materials to be cracked. Since the oil and solid components returned to the cracker It has a certain temperature, which can preheat the newly added material to be cracked, and further improve the efficiency of cracking;
  • the temperature of the non-condensable gas outlet is generally controlled to be less than 40 °C, so that The light oil components in the oil and gas can be completely condensed and stored in the second oil storage tank, and the non-condensable gas can be sent to the pressure control device after being discharged through the non-condensable gas outlet, and used as the fuel gas of the combustion furnace;
  • the flue gas purification system is directly connected with the regenerative circulating fan through a pipeline, and the pipeline is provided with a control valve and a connecting pipe connected with the heating device, so that when the flue gas temperature required by the flue gas circulating device is When it is low, the total amount of high-temperature flue gas entering the flue gas inlet pipe can be adjusted through the above control valve.
  • the excess flue gas can either be sent to other heat-using environments through the connecting pipe connected to the heating device, or directly into the flue gas. Purification system for purification.
  • the present invention adopts the multi-stage cooling and purification device for cracked oil and gas with this structure, and the oil and solid components enriched at the bottom can be sent back to the cracker through the first cooler for secondary cracking, thereby improving the cracking efficiency.
  • the purity of the cracked gas is improved through multi-stage cooling, and the comprehensive utilization of waste heat is realized.
  • Fig. 1 is the structural representation of the cracked oil and gas multi-stage cooling and purification device according to the present invention
  • Fig. 2 is the process flow diagram of the cracked oil and gas multi-stage cooling and purifying device of the present invention during operation;
  • Fig. 3 is the structural cross-sectional view of the middle part of the oil and gas condensing tower
  • a multi-stage cooling and purification device for cracked oil and gas the device includes a first cooler and a second cooler arranged in series, the two coolers have the same structure, and both include a horizontally arranged oil storage tank, The oil storage tank is connected with an oil and gas inlet tower and an oil and gas condensing tower.
  • a condensing pipeline 18 is arranged in the oil and gas condensing tower.
  • a cooling cavity 19 is arranged outside the condensing pipeline 18. The cooling medium inlet and the cooling medium outlet are connected to the cooling cavity. After the oil and gas enters the oil and gas condensing tower, it moves upward along the condensing pipeline;
  • first oil and gas inlet tower 4 is provided with a first oil and gas inlet 5 on the side, and a flue gas circulation device is connected to the first oil and gas condensing tower 17;
  • the gas inlet pipe 6 is connected to the cooling medium inlet of the first oil and gas condensing tower 17, and the flue gas return pipe 10 is connected to the cooling medium outlet of the first oil and gas condensing tower 17; the flue gas inlet pipe 6 is connected with a heat recovery cycle
  • the fan 8 is also provided with an air inlet pipe 7 between the two, and the flue gas return pipe 10 is connected with a flue gas purification system 11;
  • the oil outlet 2 at the bottom of the first oil storage tank 3 is connected to the cracker inlet through a circulating pump 1;
  • a first oil and gas outlet is provided at the top of an oil and gas condensing tower 17;
  • the flue gas purification system 11 is directly connected with the heat recovery circulating fan 8 through a pipeline, and the pipeline is provided with a control valve 9;
  • the temperature inside the tank is constant within the specified temperature range.
  • the temperature of the oil and gas discharged from the first oil and gas outlet of the first condensing tower is greater than 360 ° C.
  • the inventor sent it into the second oil and gas inlet tower of the second cooler, and in the tower
  • the oil and gas repeat the same process as the first oil and gas entering the tower, and enter the second oil and gas condensing tower after secondary elution in the second oil storage tank.
  • the cooling medium is replaced with condensed water.
  • the temperature of the non-condensable gas outlet is generally controlled to be less than 40 °C, so that The light oil components in the oil and gas can be completely condensed and stored in the second oil storage tank, and the non-condensable gas can be sent to the pressure control device after being discharged through the non-condensable gas outlet and used as the fuel gas of the combustion furnace.
  • the high-temperature oil vapor from the cracker enters the first oil and gas inlet tower through the first oil and gas inlet, and fills the tower body and finally presses down into the first oil storage tank and the pre-installed oil in the oil storage tank Contact, through which the solid components are eluted. Since the oil in the oil storage tank is not fully loaded, a cavity is left in the top of the first oil storage tank to facilitate the movement of oil and gas. After preliminary elution, the oil and gas enter the first oil storage tank. an oil and gas condensing tower;
  • the high-temperature flue gas as the heat source of the cracker enters the flue gas inlet pipe through the regenerative circulating fan, and at the same time, the low-temperature air is brought in through the air inlet pipe to reduce the temperature of the flue gas and then enter the first oil and gas condensing tower;
  • the ratio of low temperature air to high temperature flue gas is controlled to realize the control of the first oil and gas outlet temperature of the first condensing tower, generally
  • the outlet temperature is controlled to be greater than 360°C. The reason for this design is to keep the oil that can be converted into liquid within this temperature range in the first oil storage tank.
  • the secondary cracked material through this higher temperature heat exchange, converts this part of the oil and gas into liquid, which is convenient for subsequent processing, and this part of the oil in the first oil storage tank will gradually settle to the bottom of the oil tank, and The solid components eluted above are mixed, and the oil is discharged together with the solid components by a circulating pump in the later stage, and sent into the cracker.
  • the solid components can be used as heat carriers to improve the heat exchange area of the oil, and further Improve the efficiency of cracking, and the presence of oil also facilitates the discharge of solid components, reducing the difficulty of equipment operation; and the flue gas after heat exchange can enter the flue gas purification system for purification;
  • the total amount of oil converted in the above process is not large.
  • this part of the oil and solid components are regularly discharged into the cracker through the circulating pump; generally, it is controlled within 4-5 hours as In one cycle, the oil and solid components returned to the cracker can be processed together with the newly added materials to be cracked. Since the oil and solid components of the cracker have a certain temperature, they can be used for the newly added materials to be cracked. Carry out preheating to further improve the efficiency of cracking;
  • the temperature of the non-condensable gas outlet is generally controlled to be less than 40 °C, so that The light oil components in the oil and gas can be completely condensed and stored in the second oil storage tank, and the non-condensable gas can be sent to the pressure control device after being discharged through the non-condensable gas outlet, and used as the fuel gas of the combustion furnace;
  • the flue gas purification system is directly connected with the regenerative circulating fan through a pipeline, and the pipeline is provided with a control valve and a connecting pipe connected with the heating device, so that when the flue gas temperature required by the flue gas circulating device is When it is low, the total amount of high-temperature flue gas entering the flue gas inlet pipe can be adjusted through the above control valve.
  • the excess flue gas can either be sent to other heat-using environments through the connecting pipe connected to the heating device, or directly into the flue gas. Purification system for purification.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

一种裂解油气多级冷却净化装置，该装置包括串联设置的第一冷却器和第二冷却器，两个冷却器结构相同，均包括水平设置的储油罐，储油罐上连接有油气进塔和油气冷凝塔，其中第一油气进塔（4）侧面设置有第一油气进口（5），第一油气冷凝塔（17）上连接有烟气循环装置；第二油气进塔（12）顶部设置有第二油气进口，第一油气冷凝塔（17）上连接有冷却水循环装置；第一储油罐底部出油口（2）通过循环泵（1）与裂解器进口连接；采用这种结构的裂解油气多级冷却净化装置，可以通过第一冷却器将底部富集的残油送回裂解器进行二次裂解，提高裂解效率，同时通过多级冷却提高裂解气的纯度，实现余热的综合利用。

Description

一种裂解油气多级冷却净化装置 技术领域
本发明属于废弃物裂解技术领域，具体涉及一种裂解油气多级冷却净化装置。
背景技术
目前，废旧橡胶和废塑料可通过高温裂解的方式进行处理，这些高分子材料裂解后可以产生大量的可回收油气，但是这部分油气的成分较为复杂，现有技术难以对这部分油气进行合理的回收和利用，且不同来源的油气其组分各不相同，如何能够将这部分油气很好的分离，将其中的油品尽可能多的分离出来，提高油品的回收率是现有技术难以解决的问题；
同时由于裂解温度的差异，裂解获得的油气中还含有一定的可二次裂解的物质，这部分含油物质无法得到有效的回收利用，直接作为油品排出后会导致后续油品处理工段负担增大，获得的油品质量下降，同时造成裂解产物收率降低；发明人的在先申请CN201821301314.5中公开了一种裂解油品的分油冷却装置，该装置采用油气冷凝塔A中部直接送入裂解油气的方式进行进气冷凝，同样无法对上述可二次裂解的物质进行收集和处理，因此如何更好的解决上述问题成为发明人又要努力解决的技术难题之一。
发明内容
针对上述问题，本发明提出了一种裂解油气多级冷却净化装置，该装置包括串联设置的第一冷却器和第二冷却器，两个冷却器结构相同，均包括水平设置的储油罐，储油罐上连接有油气进塔和油气冷凝塔，其中第一油气进塔侧面设置有油气进口，第一油气冷凝塔上连接有烟气循环装置；第二油气进塔顶部设置有油气进口，第一油气冷凝塔上连接有冷却水循环装置；第一储油罐底部出油口通过循环泵与裂解器进口连接；采用这种结构的裂解油气多级冷却净化装置，可以通过第一冷却器将底部富集的残油送回裂解器进行二次裂解，提高裂解效率，同时通过多级冷却提高裂解气的纯度，实现余热的综合利用。
本发明的具体技术方案是：
一种裂解油气多级冷却净化装置，该装置包括串联设置的第一冷却器和第二冷却器，两个冷却器结构相同，均包括水平设置的储油罐，储油罐上连接有油气进塔和油气冷凝塔，油气冷凝塔中设置有冷凝管路，冷凝管路外侧设置冷却腔体，冷却腔体上连接有冷却介质进口和冷却介质出口，油气进入油气冷凝塔后沿冷凝管路向上运动；
其中第一油气进塔侧面设置有第一油气进口，第一油气冷凝塔上连接有烟气循环装置；所述烟气循环装置包括烟气进管和烟气回管，烟气进管连接在第一油气冷凝塔的冷却介质进口上，烟气回管连接在第一油气冷凝塔的冷却介质出口上；所述烟气进管上连接有回热循环风机，两者之间还设置有空气进管，烟气回管连接有烟气净化系统；第一储油罐底部出油口通过循环泵与裂解器进口连接；第一油气冷凝塔顶部设置有第一油气出口；
第二油气进塔顶部设置有第二油气进口，第二油气进口与第一油气冷凝塔顶部的第一油气出口通过管路直接连接；第二油气冷凝塔上连接有冷却水循环装置；所述冷却水循环装置包括冷却水进管和冷却水回管，冷却水进管连接在第二油气冷凝塔的冷却介质进口上，冷却水回管连接在第二油气冷凝塔的冷却介质出口上；第二储油罐底部出油口通过循环泵与油液储存罐连接；第二油气冷凝塔顶部设置有不凝气出口；
更进一步的，所述烟气净化系统与回热循环风机直接通过管路连接，且该管路上设置有控制阀；且每个储油罐外侧均设置有保温套，以保证储油罐内的温度恒定在规定温度范围内；
采用上述结构的裂解油气多级冷却净化装置，来自裂解器产生的高温油蒸气通过第一油气进口进入第一油气进塔，并充满塔体最终下压到第一储油罐内与储油罐内预装的油液接触，通过其洗脱其中的固体组分，由于储油罐内的油液并非满载状态，在第一储油罐内顶部留有空腔，方便油气运动，经过初步洗脱后的油气进入第一油气冷凝塔中；
此时作为裂解器热源的高温烟气通过回热循环风机进入烟气进管，同时通过空气进管带入低温空气使烟气温度降低后进入第一油气冷凝塔；在第一冷凝塔内烟气与油气逆向换热，油气温度降低，烟气温度再次升高，在这一过程中，通过控制低 温空气与高温烟气的比例，来实现第一冷凝塔第一油气出口温度的控制，一般控制该出口温度大于360℃，之所以这样设计，是为了将在这一温度区间内可以转化为液体的油液留存在第一储油罐内，这部分油液就是背景技术中提到的可二次裂解的物质，通过这种较高温度的换热，将这部分油气转化为液态，方便后续的处理，且在第一储油罐内这部分油液会逐渐沉降到油罐底部，与上述洗脱出的固体组分混合，后期通过循环泵将这部分油液与固体组分一起排出，送入裂解器内，此时固体组分可以作为热载体提高油液的换热面积，进一步提高裂解的效率，而油液的存在也方便固体组分的排出，降低了设备的运行难度；而换热后的烟气则可以进入烟气净化系统进行净化；
由于上述过程中转化出的油液总量不大，一般控制整个设备运行一段时间后，定期通过循环泵将这部分油液与固体组分一起排出送入裂解器；这一时间一般控制在4-5小时为一个周期，也可以根据具体的工况进行调整，返回裂解器的油液和固体组分可以与新加入的待裂解物料一起进行处理，由于返回裂解器的油液和固体组分自身带有一定的温度，可以为新加入的待裂解物料进行预热，进一步提高裂解的效率；
第一冷凝塔第一油气出口排出的油气温度大于360℃，为了将其中的轻油组分更快的冷凝，发明人将其送入第二冷却器的第二油气进塔，在该塔内油气重复与第一油气进塔相同的过程，并在第二储油罐内进行二次洗脱之后进入第二油气冷凝塔，此时为了提高换热效率和速度，第二油气冷凝塔内的冷却介质更换为冷凝水，通过控制冷凝水的流量以及不凝气出口出口流量，确保冷凝的效果，通过第二油气冷凝塔的冷却，控制不凝气出口的温度一般控制在小于40℃，这样可以将油气中的轻油组分完全冷凝并储存在第二储油罐内，而不凝气通过不凝气出口排出后可送入压力控制装置，并作为燃烧炉的燃料气使用；
上述装置中，在烟气净化系统与回热循环风机直接通过管路连接，且该管路上设置有控制阀，以及与供热装置连接的连接管，这样当烟气循环装置需要的烟气温度较低时，可以通过上述控制阀调配进入烟气进管的高温烟气总量，多余的烟气既可以通过与供热装置连接的连接管送入其他用热环境，也可以直接进入烟气净化系统进行净化处理。
综上所述，本发明采用这种结构的裂解油气多级冷却净化装置，可以通过第一冷却器将底部富集的油液和固体组分送回裂解器进行二次裂解，提高裂解效率，同时通过多级冷却提高裂解气的纯度，实现余热的综合利用。
附图说明
图1为本发明所述裂解油气多级冷却净化装置的结构示意图；
图2为本发明所述裂解油气多级冷却净化装置运作时的工艺流程图；
图3为油气冷凝塔中部的结构剖视图；
图中1为循环泵，2为第一储油罐底部出油口，3为第一储油罐，4为第一油气进塔，5为第一油气进口，6为烟气进管，7为空气进管，8为回热循环风机，9为控制阀，10为烟气回管，11为烟气净化系统，12为第二油气进塔，13为冷却水回管，14为第二油气冷凝塔，15为冷却水进管，16为第二储油罐底部出油口，17为第一油气冷凝塔，18为冷凝管路，19为冷却腔体。
具体实施方式
以下通过实施例形式的具体实施方式，对本发明的上述内容做进一步的详细说明，凡基于本发明上述内容所实现的技术均属于本发明的范围。
实施例1
如图1和3所示，一种裂解油气多级冷却净化装置，该装置包括串联设置的第一冷却器和第二冷却器，两个冷却器结构相同，均包括水平设置的储油罐，储油罐上连接有油气进塔和油气冷凝塔，油气冷凝塔中设置有冷凝管路18，冷凝管路18外侧设置冷却腔体19，冷却腔体上连接有冷却介质进口和冷却介质出口，油气进入油气冷凝塔后沿冷凝管路向上运动；
其中第一油气进塔4侧面设置有第一油气进口5，第一油气冷凝塔17上连接有烟气循环装置；所述烟气循环装置包括烟气进管6和烟气回管10，烟气进管6连接在第一油气冷凝塔17的冷却介质进口上，烟气回管10连接在第一油气冷凝塔17的冷却介质出口上；所述烟气进管6上连接有回热循环风机8，两者之间还设置 有空气进管7，烟气回管10连接有烟气净化系统11；第一储油罐3底部出油口2通过循环泵1与裂解器进口连接；第一油气冷凝塔17顶部设置有第一油气出口；
第二油气进塔12顶部设置有第二油气进口，第二油气进口与第一油气冷凝塔顶部的第一油气出口通过管路直接连接；第二油气冷凝塔14上连接有冷却水循环装置；所述冷却水循环装置包括冷却水进管15和冷却水回管13，冷却水进管15连接在第二油气冷凝塔14的冷却介质进口上，冷却水回管13连接在第二油气冷凝塔14的冷却介质出口上；第二储油罐底部出油口16通过循环泵与油液储存罐连接；第二油气冷凝塔14顶部设置有不凝气出口；
更进一步的，所述烟气净化系统11与回热循环风机8直接通过管路连接，且该管路上设置有控制阀9；且每个储油罐外侧均设置有保温套，以保证储油罐内的温度恒定在规定温度范围内。
实施例2
采用实施例1所述裂解油气多级冷却净化装置进行油气冷却净化的工艺，具体过程如下：
来自裂解器产生的高温油蒸气通过第一油气进口进入第一油气进塔，并充满塔体最终下压到第一储油罐内与储油罐内预装的油液接触，通过其洗脱其中的固体组分，由于储油罐内的油液并非满载状态，在第一储油罐内顶部留有空腔，方便油气运动，经过初步洗脱后的油气进入第一油气冷凝塔中；
此时作为裂解器热源的高温烟气通过回热循环风机进入烟气进管，同时通过空气进管带入低温空气使烟气温度降低后进入第一油气冷凝塔；在第一冷凝塔内烟气与油气逆向换热，油气温度降低，烟气温度再次升高，在这一过程中，通过控制低温空气与高温烟气的比例，来实现第一冷凝塔第一油气出口温度的控制，一般控制该出口温度大于360℃，之所以这样设计，是为了将在这一温度区间内可以转化为液体的油液留存在第一储油罐内，这部分油液就是背景技术中提到的可二次裂解的物质，通过这种较高温度的换热，将这部分油气转化为液态，方便后续的处理，且在第一储油罐内这部分油液会逐渐沉降到油罐底部，与上述洗脱出的固体组分混合，后期通过循环泵将这部分油液与固体组分一起排出，送入裂解器内；
第一冷凝塔第一油气出口排出的油气温度大于360℃，为了将其中的轻油组分更快的冷凝，发明人将其送入第二冷却器的第二油气进塔，在该塔内油气重复与第一油气进塔相同的过程，并在第二储油罐内进行二次洗脱之后进入第二油气冷凝塔，此时为了提高换热效率和速度，第二油气冷凝塔内的冷却介质更换为冷凝水，通过控制冷凝水的流量以及不凝气出口出口流量，确保冷凝的效果，通过第二油气冷凝塔的冷却，控制不凝气出口的温度一般控制在小于40℃，这样可以将油气中的轻油组分完全冷凝并储存在第二储油罐内，而不凝气通过不凝气出口排出后可送入压力控制装置，并作为燃烧炉的燃料气使用。
实施例3
采用实施例1所述裂解油气多级冷却净化装置进行油气冷却净化的工艺，具体过程如下：
如图2所示，来自裂解器产生的高温油蒸气通过第一油气进口进入第一油气进塔，并充满塔体最终下压到第一储油罐内与储油罐内预装的油液接触，通过其洗脱其中的固体组分，由于储油罐内的油液并非满载状态，在第一储油罐内顶部留有空腔，方便油气运动，经过初步洗脱后的油气进入第一油气冷凝塔中；
此时作为裂解器热源的高温烟气通过回热循环风机进入烟气进管，同时通过空气进管带入低温空气使烟气温度降低后进入第一油气冷凝塔；在第一冷凝塔内烟气与油气逆向换热，油气温度降低，烟气温度再次升高，在这一过程中，通过控制低温空气与高温烟气的比例，来实现第一冷凝塔第一油气出口温度的控制，一般控制该出口温度大于360℃，之所以这样设计，是为了将在这一温度区间内可以转化为液体的油液留存在第一储油罐内，这部分油液就是背景技术中提到的可二次裂解的物质，通过这种较高温度的换热，将这部分油气转化为液态，方便后续的处理，且在第一储油罐内这部分油液会逐渐沉降到油罐底部，与上述洗脱出的固体组分混合，后期通过循环泵将这部分油液与固体组分一起排出，送入裂解器内，此时固体组分可以作为热载体提高油液的换热面积，进一步提高裂解的效率，而油液的存在也方便固体组分的排出，降低了设备的运行难度；而换热后的烟气则可以进入烟气净化系统进行净化；
上述过程中转化出的油液总量不大，一般控制整个设备运行一段时间后，定期通过循环泵将这部分油液与固体组分一起排出送入裂解器；一般控制在4-5小时为一个周期，返回裂解器的油液和固体组分可以与新加入的待裂解物料一起进行处理，由于裂解器的油液和固体组分自身带有一定的温度，可以为新加入的待裂解物料进行预热，进一步提高裂解的效率；
第一冷凝塔第一油气出口排出的油气温度大于360℃，为了将其中的轻油组分更快的冷凝，发明人将其送入第二冷却器的第二油气进塔，在该塔内油气重复与第一油气进塔相同的过程，并在第二储油罐内进行二次洗脱之后进入第二油气冷凝塔，此时为了提高换热效率和速度，第二油气冷凝塔内的冷却介质更换为冷凝水，通过控制冷凝水的流量以及不凝气出口出口流量，确保冷凝的效果，通过第二油气冷凝塔的冷却，控制不凝气出口的温度一般控制在小于40℃，这样可以将油气中的轻油组分完全冷凝并储存在第二储油罐内，而不凝气通过不凝气出口排出后可送入压力控制装置，并作为燃烧炉的燃料气使用；
上述装置中，在烟气净化系统与回热循环风机直接通过管路连接，且该管路上设置有控制阀，以及与供热装置连接的连接管，这样当烟气循环装置需要的烟气温度较低时，可以通过上述控制阀调配进入烟气进管的高温烟气总量，多余的烟气既可以通过与供热装置连接的连接管送入其他用热环境，也可以直接进入烟气净化系统进行净化处理。

Claims (6)

  1. 一种裂解油气多级冷却净化装置，其特征在于：包括串联设置的第一冷却器和第二冷却器，两个冷却器结构相同，均包括水平设置的储油罐，储油罐上连接有油气进塔和油气冷凝塔，油气冷凝塔中设置有冷凝管路，冷凝管路外侧设置冷却腔体，冷却腔体上连接有冷却介质进口和冷却介质出口，油气进入油气冷凝塔后沿冷凝管路向上运动。
  2. 根据权利要求1所述裂解油气多级冷却净化装置，其特征在于：第一油气进塔(4)侧面设置有第一油气进口(5)，第一油气冷凝塔(17)上连接有烟气循环装置；所述烟气循环装置包括烟气进管(6)和烟气回管(10)，烟气进管(6)连接在第一油气冷凝塔(17)的冷却介质进口上，烟气回管(10)连接在第一油气冷凝塔(17)的冷却介质出口上；所述烟气进管(6)上连接有回热循环风机(8)，两者之间还设置有空气进管(7)，烟气回管(10)连接有烟气净化系统(11)；第一油气冷凝塔(17)顶部设置有第一油气出口；第二油气进塔(12)顶部设置有第二油气进口，第二油气进口与第一油气冷凝塔顶部的第一油气出口通过管路直接连接；第二油气冷凝塔(14)上连接有冷却水循环装置；所述冷却水循环装置包括冷却水进管(15)和冷却水回管(13)，冷却水进管(15)连接在第二油气冷凝塔(14)的冷却介质进口上，冷却水回管(13)连接在第二油气冷凝塔(14)的冷却介质出口上；第二油气冷凝塔(14)顶部设置有不凝气出口。
  3. 根据权利要求2所述裂解油气多级冷却净化装置，其特征在于：第一储油罐底部出油口(2)通过循环泵(1)与裂解器进口连接。
  4. 根据权利要求2所述裂解油气多级冷却净化装置，其特征在于：第二储油罐底部出油口(16)通过循环泵与油液储存罐连接。
  5. 根据权利要求2所述裂解油气多级冷却净化装置，其特征在于：所述烟气净化系统(11)与回热循环风机(8)直接通过管路连接，且该管路上设置有控制阀(9)。
  6. 根据权利要求1所述裂解油气多级冷却净化装置，其特征在于：所述储油罐外侧设置有保温套。
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