WO2022082621A1 - 一种加氢强化微界面系统 - Google Patents

一种加氢强化微界面系统 Download PDF

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Publication number
WO2022082621A1
WO2022082621A1 PCT/CN2020/122876 CN2020122876W WO2022082621A1 WO 2022082621 A1 WO2022082621 A1 WO 2022082621A1 CN 2020122876 W CN2020122876 W CN 2020122876W WO 2022082621 A1 WO2022082621 A1 WO 2022082621A1
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Prior art keywords
hydrogenation
hydrogenation reactor
micro
liquid
side wall
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PCT/CN2020/122876
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English (en)
French (fr)
Inventor
张志炳
周政
张锋
李磊
孟为民
王宝荣
杨高东
罗华勋
杨国强
田洪舟
曹宇
Original Assignee
南京延长反应技术研究院有限公司
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Publication of WO2022082621A1 publication Critical patent/WO2022082621A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B08—CLEANING
    • B08B—CLEANING IN GENERAL; PREVENTION OF FOULING IN GENERAL
    • B08B9/00—Cleaning hollow articles by methods or apparatus specially adapted thereto 
    • B08B9/08—Cleaning containers, e.g. tanks
    • B08B9/093—Cleaning containers, e.g. tanks by the force of jets or sprays
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/002—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the feeding side being of particular interest

Definitions

  • the invention relates to the field of oil hydrogenation, in particular to a hydrogenation strengthening micro-interface system.
  • the existing hydrogenation reactor requires a lot of manpower in the process of maintenance and cleaning, including entering the hydrogenation reactor through the manhole for washing and on-site operation of various pipeline valves. This not only increases labor costs, but also reduces the safety of production.
  • the purpose of the present invention is to provide a hydrogenation-enhanced micro-interface system.
  • the hydrogenation-enhanced micro-interface system is provided with a liquid injector in the hydrogenation reactor.
  • the liquid injector can efficiently crush the water for cleaning the hydrogenation reactor. It is formed into micron-sized droplets, and the ejector collides with the top of the hydrogenation reactor to replace manual cleaning, so as to achieve the effect of improving mass transfer.
  • the invention provides a hydrogenation strengthening micro-interface system, comprising: a hydrogenation reactor;
  • the middle area of the bottom surface of the hydrogenation reactor protrudes upward to form a plane, and the flat parts on both sides of the protruding plane of the bottom surface of the hydrogenation reactor are respectively provided with liquid outlets, and the sidewall of the hydrogenation reactor is provided with There are a liquid inlet and a product outlet, the side wall of the hydrogenation reactor is provided with a raw material inlet for entering oil products, and the raw material inlet is arranged at a lower position of the side wall of the hydrogenation reactor;
  • the inner upper part and the side wall of the hydrogenation reactor are provided with a liquid injector, the bottom of the liquid injector is a plane, the top is a semicircular arc surface, and several semicircular arc surfaces are arranged in sequence.
  • the injection port, the injection direction of the injection port of the liquid injector located in the upper part is toward the top of the hydrogenation reactor, and the injection direction of the injection port of the liquid injector located in the side wall is toward the opposite side wall of the hydrogenation reactor,
  • the liquid inlet is connected to the bottom of the liquid injector through a pipeline, and the raw material inlet is connected to the bottom of the liquid injector;
  • the product outlet is connected to the refining hydrogenation reactor for deep hydrogenation reaction, and the gas phase separated from the reaction product from the bottom of the refining hydrogenation reactor enters the desulfurization tower to realize the absorption of hydrogen sulfide in the gas phase.
  • the hydrogenation reactor requires a lot of manpower in the process of overhauling and cleaning, including entering the hydrogenation reactor through manholes for washing and on-site operation of various pipeline valves. This not only increases labor costs, but also reduces the safety of production.
  • the present invention provides a hydrogenation-enhanced micro-interface system with a specific structure. Broken to form a mist, thereby improving the spraying effect and correspondingly improving the mass transfer effect.
  • the oil from the raw material inlet is also efficiently broken into mist through the injection port on the liquid injector, thereby increasing the contact area between the oil and hydrogen, thereby improving the reaction efficiency of hydrogen.
  • the reason why the center of the bottom of the hydrogenation reactor is raised is to efficiently discharge the materials in the hydrogenation reactor from the liquid outlet. If the bottom is flat, there will be a small amount of material remaining, so it is best to follow the The solution of the present invention is implemented so that the center position of the bottom of the hydrogenation reactor is raised upward to form a plane.
  • the protrusions are in a semi-circular arc shape, which can further reduce the possibility of fluid accumulation.
  • the liquid outlet is set into a conical structure, which can accelerate the discharge of materials.
  • a mesh surface with a plurality of micropores evenly distributed is laid in each of the jetting openings.
  • the liquid ejector of the present invention is mainly connected with the liquid port through a pipeline, and the cleaning water is introduced into the liquid ejector and sprayed out through the ejection port on the semicircular arc surface of the liquid ejector.
  • the reason why it is designed as a semicircle The structure of the arc-shaped surface is to improve the cleaning effect and ensure that the sprayed cleaning water can clean the wall surface of the hydrogenation reactor in an all-round way. In this way, after the water sprayed out is broken and dispersed, it becomes mist to improve the mass transfer effect, which is also equivalent to the corresponding effect of the micro-interface generator.
  • the side wall of the hydrogenation reactor is provided with a raw material inlet for entering the oil, and the oil to be hydrogenated is introduced into the hydrogenation reactor through the raw material inlet, and the hydrogenation reaction is carried out with the introduced hydrogen to obtain hydrodesulfurization. After the oil, to ensure the quality of the product.
  • the liquid inlet is connected to the central position of the bottom of the liquid ejector through a pipeline, so that the incoming liquid just enters from the middle of the liquid ejector, and the liquid can be ejected more uniformly.
  • the raw material inlet is connected to the center of the bottom of the liquid injector through a pipeline, so that the incoming oil just enters from the middle of the liquid injector, and the liquid can be sprayed out more uniformly.
  • the oil itself has a relatively high viscosity. The spray effect may not reach the spray effect of cleaning water.
  • a stirring paddle is provided at the center bulge of the inner bottom of the hydrogenation reactor to accelerate the discharge.
  • the stirring paddle is also arranged in the raised position to improve the discharge efficiency of the fermentation product, and the fermentation efficiency can also be improved by stirring.
  • two stirring paddles are arranged side by side at the protruding plane at the bottom of the hydrogenation reactor.
  • a desulfurization agent storage tank is arranged on the side of the desulfurization tower, the desulfurization agent storage tank is connected with the lower part of the side wall of the desulfurization tower through a pipeline, and the top of the desulfurization agent storage tank is connected with the desulfurization agent through a pipeline. the spray line connection.
  • the desulfurizing agent is generally lye, which is circulated into the desulfurization tower and is in reverse contact with the gas phase entering from the bottom of the desulfurization tower, sprayed and absorbed to achieve desulfurization, and the lye after desulfurization is returned to the desulfurizer storage tank. In the case of serious pollution during the recycling of the lye in the storage tank, it should be stopped for replacement.
  • the desulfurizing agent spraying pipelines are in three rows, and the desulfurizing agent spraying pipelines in each row are arranged parallel to each other.
  • the absorption effect of the desulfurizer on hydrogen sulfide in the gas phase can be improved.
  • a micro-interface generator can also be arranged in the hydrogenation reactor, and the micro-interface generator is arranged directly below the liquid injector, and the micro-interface generator is used in combination with the liquid injector to improve the synergistic effect between the two.
  • the number of the micro-interface generators is single, and its specific type is preferably a pneumatic micro-interface generator, because the pneumatic type is relatively low in cost and easy to install.
  • an air inlet for entering hydrogen is provided on the side wall of the hydrogenation reactor, and the air inlet is connected to the side wall of the desulfurization tower for recycling the purified hydrogen.
  • the air inlet is connected to the micro-interface generator through a pipe.
  • the reaction product from the refining hydrogenation reactor is recovered in the liquid phase
  • the gas phase is sent to the desulfurization tower for desulfurization.
  • the components in the gas phase are mainly hydrogen sulfide and hydrogen. After the hydrogen sulfide is absorbed in the desulfurization tower, the hydrogen is removed from the
  • the air inlet connected to the desulfurization tower enters into the micro-interface generator, and contacts the oil product from the raw material inlet for dispersion and crushing.
  • the micro-interface generator in the hydrogenation reactor breaks the air into micro-scale micro-bubbles and releases the micro-bubbles into the interior to increase the mass transfer area of the phase boundary between the raw materials during the reaction process, so that the two phases are fully contacted.
  • the concentration of dissolved gas in the liquid phase is increased, the efficiency is improved, and the reaction time is shortened.
  • micro-interface generator used in the present invention has been embodied in the inventor's prior patents, such as application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660, CN105903425A, Patents of CN109437390A, CN205833127U and CN207581700U.
  • application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660, CN105903425A, Patents of CN109437390A, CN205833127U and CN207581700U In the previous patent CN201610641119.6, the specific product structure and working principle of the micro-bubble generator (that is, the micro-interface generator) were introduced in detail.
  • the body is provided with an inlet communicating with the cavity, the opposite first and second ends of the cavity are open, wherein the cross-sectional area of the cavity is from the middle of the cavity to the first and second ends of the cavity.
  • the second end is reduced; the secondary crushing piece is arranged at at least one of the first end and the second end of the cavity, a part of the secondary crushing piece is arranged in the cavity, and both ends of the secondary crushing piece and the cavity are open
  • An annular channel is formed between the through holes of the micro-bubble generator.
  • the micro-bubble generator also includes an air inlet pipe and a liquid inlet pipe.” From the specific structure disclosed in the application document, we can know that its specific working principle is: the liquid enters the micron tangentially through the liquid inlet pipe. In the bubble generator, ultra-high-speed rotation and cutting of the gas make the gas bubbles break into micro-bubbles at the micron level, thereby increasing the mass transfer area between the liquid phase and the gas phase, and the micro-bubble generator in this patent belongs to the pneumatic micro-interface generation. device.
  • the previous patent 201610641251.7 records that the primary bubble breaker has a circulating liquid inlet, a circulating gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker communicates the feed port with the gas-liquid mixture outlet, indicating that the bubble breaker is both It needs to be mixed with gas and liquid.
  • the primary bubble breaker mainly uses circulating liquid as power, so in fact, the primary bubble breaker belongs to the hydraulic micro-interface generator, and the secondary bubble breaker is a gas-liquid breaker. The mixture is simultaneously fed into the elliptical rotating ball for rotation, so that the bubbles are broken during the rotation, so the secondary bubble breaker is actually a gas-liquid linkage type micro-interface generator.
  • both hydraulic micro-interface generators and gas-liquid linkage micro-interface generators belong to a specific form of micro-interface generators.
  • the micro-interface generators used in the present invention are not limited to the above-mentioned forms.
  • the specific structure of the bubble breaker described in the prior patent is only one of the forms that the micro-interface generator of the present invention can take.
  • the previous patent 201710766435.0 recorded that "the principle of the bubble breaker is to achieve high-speed jets to achieve gas collision", and also stated that it can be used in micro-interface enhanced reactors to verify the relationship between the bubble breaker and the micro-interface generator.
  • the top of the bubble breaker is the liquid phase inlet, and the side is the gas phase inlet.
  • the liquid phase entering from the top provides the entrainment power, so as to achieve the effect of crushing into ultra-fine bubbles, which can also be seen in the accompanying drawings.
  • the bubble breaker has a conical structure, and the diameter of the upper part is larger than that of the lower part, so that the liquid phase can provide better entrainment power.
  • micro-interface generator Since the micro-interface generator was just developed in the early stage of the previous patent application, it was named as micro-bubble generator (CN201610641119.6), bubble breaker (201710766435.0), etc., and later changed its name to micro-interface generator with continuous technological improvement.
  • the micro-interface generator in the present invention is equivalent to the previous micro-bubble generator, bubble breaker, etc., but the names are different.
  • the micro-interface generator of the present invention belongs to the prior art, although some micro-interface generators belong to the type of pneumatic micro-interface generators, some micro-interface generators belong to the type of hydraulic micro-interface generators, and some are of the type of hydraulic micro-interface generators. It belongs to the type of gas-liquid linkage micro-interface generator, but the difference between the types is mainly selected according to the specific working conditions.
  • the connection between the micro-interface generator and the reactor and other equipment including the connection structure, connection position, It depends on the structure of the micro-interface generator, which is not limited.
  • the hydrogenation-enhanced micro-interface system of the present invention is provided with a liquid injector in the hydrogenation reactor.
  • the liquid injector can efficiently break the water for cleaning the hydrogenation reactor into micron-sized droplets, and pass the injector.
  • the upper part of the impact hydrogenation reactor is replaced by manual cleaning, and the liquid ejector can also be applied to the injection of raw materials into the hydrogenation reactor, so as to achieve the effect of improving the reaction mass transfer;
  • the hydrogenation strengthening micro-interface system of the present invention can realize the cooperation between the liquid ejector and the micro-interface generator, so that the micro-interface generator can break the air into micro-sized micro-bubbles and release the micro-bubbles into the interior , in order to increase the mass transfer area of the phase boundary between the raw materials in the reaction process, so that the two phases are fully contacted, the concentration of dissolved gas in the liquid phase is increased, the efficiency is improved, and the reaction time is shortened.
  • Fig. 1 is the structural representation of the hydrogenation strengthening micro-interface system provided in the embodiment of the present invention
  • FIG. 2 is a schematic structural diagram of a mesh surface of a hydrogenation-enhanced micro-interface system provided by an embodiment of the present invention.
  • the terms “installed”, “connected” and “connected” should be understood in a broad sense, unless otherwise expressly specified and limited, for example, it may be a fixed connection or a detachable connection Connection, or integral connection; may be mechanical connection or electrical connection; may be direct connection or indirect connection through an intermediate medium, and may be internal communication between two elements.
  • installed may be a fixed connection or a detachable connection Connection, or integral connection; may be mechanical connection or electrical connection; may be direct connection or indirect connection through an intermediate medium, and may be internal communication between two elements.
  • FIG. 1 it is a hydrogenation strengthening micro-interface system according to an embodiment of the present invention, which mainly includes a hydrogenation reactor 10, a refining hydrogenation reactor 20, a desulfurization tower 30 and a desulfurization agent storage tank 40; the hydrogenation reactor 10
  • the upper inner part and the side wall are provided with a liquid injector 103, and a micro-interface generator 105 is also provided in the hydrogenation reactor.
  • the side wall is provided with a liquid inlet 101 and a product outlet, and is also provided with an air inlet 106 for entering hydrogen.
  • the side wall of the hydrogenation reactor 10 is also provided with a raw material inlet 107 for entering oil, and the raw material inlet 107 is provided
  • the hydrogenation reactor 10 is located at the lower side of the side wall, so that the raw material inlet 107 is relatively close to the air inlet 106, and the incoming oil can come into contact with the hydrogen, thereby improving the crushing and dispersing effect of the hydrogen.
  • the liquid injector 103 on the upper part is connected with the liquid inlet 101 through a pipeline, the liquid injector 103 located on the side wall is connected with the raw material inlet 107 through a pipeline, the bottom of the liquid injector 103 is a plane, and the top surface is a semicircular arc surface, Several injection ports 1031 are arranged on the semicircular arc surface in sequence, the injection port 1031 located on the upper part is directed toward the top of the hydrogenation reactor 10, and the injection port 1031 located on the side wall is directed toward the hydrogenation reaction
  • the liquid inlet 101 is connected to the bottom of the liquid injector 103 through a pipeline, preferably by connecting with the bottom center of the liquid injector 103, by breaking the liquid entering the liquid injector 103 into a diameter of micrometers.
  • microdroplets are ejected from the ejection port 1031 raised on the surface to collide with the top of the hydrogenation reactor for efficient cleaning.
  • a mesh surface 1032 with a plurality of micropores evenly distributed in the spray port 1031 is laid.
  • the number of mesh surfaces 1032 is not limited. See Figure 2 for details.
  • the number of micro-interface generators 105 is single, and the gas inlet 106 is connected to the side wall of the desulfurization tower 30 for returning the purified hydrogen to the hydrogenation reactor for recycling, and the gas inlet 106 is connected to the gas inlet 106 through a pipeline.
  • the corresponding micro-interface generator 105 is connected.
  • the bottom of the hydrogenation reactor 10 is provided with a liquid outlet 102 for discharging the materials accumulated at the bottom of the hydrogenation reactor 10 .
  • Both sides of the bottom of the hydrogenation reactor 10 are flat, and the center position is raised upward to be a plane.
  • the liquid outlets 102 are respectively provided at the flat positions on both sides of the bottom of the hydrogenation reactor 10, and the liquid outlets 102 are used for discharging waste liquid.
  • the inner bottom center of the hydrogenation reactor 10 is provided with a stirring paddle 104 to accelerate the discharge, and the direction of the blades is upward, so as to be used for stirring at the bottom of the hydrogenation reactor 10 when flushing and draining. It can be adjusted steplessly.
  • a desulfurization agent storage tank 40 is provided on the side of the desulfurization tower 30, the desulfurization agent storage tank 40 is connected with the lower part of the side wall of the desulfurization tower 30 through a pipeline, and the top of the desulfurization agent storage tank 40 is connected with the desulfurization agent spray pipeline through a pipeline, There are three rows of desulfurization agent spraying pipelines, and each row of desulfurization agent spraying pipelines is arranged in parallel with each other.
  • This embodiment also includes a PLC (or DCS, PLC and DCS) control system: connected to the sensor of the hydrogenation reactor 10, for intelligently controlling process operations and parameters, realizing remote control of production, in line with the intelligentization of production .
  • PLC or DCS, PLC and DCS
  • the cleaning water above the hydrogenation reactor 10 is transported to the inside of the liquid ejector 103 through the liquid inlet 101 and sprayed out through the jetting port 1031 on the arc surface, and is efficiently broken into microns through the mesh surface 1032
  • the liquid droplets of the order (1 ⁇ m ⁇ d ⁇ 1 mm) are ejected from the protruding ejection port 1031 on the surface of the liquid ejector 103 , collide with the top of the hydrogenation reactor 10 and clean the top.
  • the cleaned droplets form a liquid level at the bottom of the tank.
  • the installation direction of the blades of the stirring paddle 104 is downward, the liquid above the blades will be pumped to the two sides below, and vortices will be formed on both sides of the stirring paddle 104 to wash and clean both sides of the lower part of the hydrogenation reactor 10 .
  • the water channel below is opened, and the input water flow cleans the side wall of the hydrogenation reactor under the action of the stirring paddle 104, closes the water delivery valve after flushing for 30 minutes, reduces the rotational speed to 100rpm/min, and passes through the lower end of the hydrogenation reactor 10.
  • the liquid outlets 102 on both sides discharge water, close the liquid outlets 102, and reduce the rotational speed to 50 rpm/min.
  • the operation and process parameters in the working process of the above-mentioned hydrogenation enhanced micro-interface system are completely controlled by the control system of PLC (or DCS, PLC and DCS), and the control system is connected with each sensor on the hydrogenation reactor 10 to realize automatic intelligent control , saving labor costs.
  • the pressure of the above hydrogenation reaction is 2-8MPa, and the temperature of the hydrogenation reaction is 250-320°C. Most preferably, the pressure of the hydrogenation reaction is 3.5 MPa, and the temperature of the hydrogenation reaction is 300°C.
  • the pressure of the refining hydrogenation reaction is 2-8MPa, and the temperature of the refining hydrogenation reaction is 250-320°C. Most preferably, the pressure of the refining hydrogenation reaction is 3.5MPa, and the temperature of the refining hydrogenation reaction is 300°C.
  • the catalyst used in both the hydrogenation reaction and the refining hydrogenation reaction is a Mo-Ni type catalyst, and the volume ratio of the catalyst dosage in the hydrogenation reactor 10 and the refining hydrogenation reactor 20 can be (1:12)-(1:15) , preferably 1:13.
  • the solution of the present invention realizes not only the dispersion and crushing of the liquid phase, but also the dispersion and crushing of the gas phase through the cooperation of the liquid ejector and the micro-interface generator. particles, so as to improve the mass transfer effect of the system.

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Abstract

本发明提供了一种加氢强化微界面系统，包括：所述加氢反应器的底面中间区域向上凸起呈平面，在所述加氢反应器底面凸起平面的两侧平整部分别设置有出液口，所述加氢反应器的侧壁上设置有进液口以及产物出口，所述加氢反应器的侧壁设置有用于进入油品的原料进口，所述原料进口设置在所述加氢反应器侧壁靠下的位置；所述加氢反应器内上部以及侧壁均设置有液体喷射器，所述液体喷射器的底部为平面，顶部呈半圆形弧面，所述半圆形弧面上依次排布有若干个喷射口。本发明的加氢强化微界面系统节省了清洗、现场操作的成本。

Description

一种加氢强化微界面系统 技术领域
本发明涉及油品加氢领域，具体而言，涉及一种加氢强化微界面系统。
背景技术
随着人们环保意识的提高以及环保法规的日益严格，生产和使用清洁车用燃料越来越成为一种发展趋势，油品深度加氢脱硫技术的开发则成为了目前研究的热点。目前，大多加氢精制装置操作流程是原料油通过同精制油、反应产物换热，并经加热炉加热至反应要求温度后进行加氢，这种加氢过程虽然操作方便，容易产业化，但是能耗高，加氢反应器压力高、温度高，产能也比较低，投资成本高。
并且，现有加氢反应器在检修清洗的过程中需要大量的人力，包括通过人孔进入加氢反应器内部洗刷以及各管路阀门的现场操作等。这样既提高了人力成本，同时降低了生产的安全性。
有鉴于此，特提出本发明。
发明内容
本发明的目的在于提供一种加氢强化微界面系统，该加氢强化微界面系统通过在加氢反应器内设置液体喷射器，一方面液体喷射器可将清洗加氢反应器的水高效破碎成微米级液滴，并通过喷射器冲撞加氢反应器上方取代人工进行清洗，从而达到提高传质的效果。
为了实现本发明的上述目的，特采用以下技术方案：
本发明提供了一种加氢强化微界面系统，包括：加氢反应器；
所述加氢反应器的底面中间区域向上凸起呈平面，在所述加氢反应器底面 凸起平面的两侧平整部分别设置有出液口，所述加氢反应器的侧壁上设置有进液口以及产物出口，所述加氢反应器的侧壁设置有用于进入油品的原料进口，所述原料进口设置在所述加氢反应器侧壁靠下的位置；
所述加氢反应器内上部以及侧壁均设置有液体喷射器，所述液体喷射器的底部为平面，顶部呈半圆形弧面，所述半圆形弧面上依次排布有若干个喷射口，位于上部的液体喷射器的所述喷射口的喷射方向朝向加氢反应器的顶部，位于侧壁的液体喷射器的所述喷射口的喷射方向朝向加氢反应器的对侧壁，所述进液口通过管道与所述液体喷射器的底部连接，所述原料进口与所述液体喷射器的底部连接；
所述产物出口连接精制加氢反应器进行深度加氢反应，从所述精制加氢反应器底部出来的反应产物分离出的气相进入脱硫塔中，以实现对气相中硫化氢的吸收。
现有技术中，加氢反应器在检修清洗的过程中需要大量的人力，包括通过人孔进入加氢反应器内部洗刷以及各管路阀门的现场操作等。这样既提高了人力成本，同时降低了生产的安全性。
本发明为了提高加氢强化微界面系统的清洗效果，提供了一种具有特定结构的加氢强化微界面系统，主要依靠设置在半圆形弧面上的喷射口喷射过程中将清洗水进行高效破碎形成雾状，从而提高喷淋效果，也相应的提高传质效果。另外，为了提高加氢的处理效果，从原料进口进来的油品也通过液体喷射器上的喷射口进行高效破碎成雾状，从而提高油品与氢气的接触面积，从而提高氢气的反应效率。
另外，加氢反应器的底部中心位置向上凸起的原因是为了将加氢反应器内的物料高效的从出液口排出，如果底部均为平整的会有少部分物料残留，所以最好按照本发明的方案来实施将加氢反应器底部的中心位置向上凸起呈平面。当然更优地方式是凸起呈半圆弧形，这样更能降低积液的可能性。并且出液口设置成锥形的结构更能加速物料的排出。
优选地，每个所述喷射口内铺设有均布多个微孔的网面。
本发明的液体喷射器主要是跟进液口通过管道连接，通过将清洗水引入到液体喷射器中，并通过液体喷射器半圆形弧面上的喷射口喷射出去，之所以设计成半圆形弧面的结构是为了提高清洗效果，保证喷射出去的清洗水能够对加氢反应器的壁面进行全方位的清洗，此外优选地，每个所述喷射口内铺设有均布多个微孔的网面，这样喷射出去的水被打碎分散后，成雾状以提高传质效果，也相当于起到了微界面发生器相应的效果。
加氢反应器的侧壁设置有进入油品的原料进口，将待加氢的油品通过原料进口通入到加氢反应器中，与通入的氢气进行加氢反应，以得到加氢脱硫后的油品，保证了产品的质量。
优选地，所述进液口通过管道与所述液体喷射器底部中心位置连接，这样进入的液体正好从液体喷射器的中部进入，能够更加均匀的喷射出液体。
优选地，所述原料进口通过管道与所述液体喷射器底部中心位置连接，这样进入的油品正好从液体喷射器的中部进入，能够更加均匀的喷射出液体，当然本身油品粘度比较大，其喷射效果可能达不到清洗水的喷射效果。
优选地，所述加氢反应器内底部中心凸起处设置有搅拌桨以起到加速排料的作用。凸起的位置设置搅拌桨也是为了提高发酵产物排出的效率，而且通过搅拌还能提升发酵效率。
为了提高搅拌效果，优选地搅拌桨的数量为两个，并排设置在所述加氢反应器底部凸起平面处。
优选地，所述脱硫塔的旁侧设置有脱硫剂储罐，所述脱硫剂储罐与所述脱硫塔的侧壁下部通过管道连接，所述脱硫剂储罐的顶部通过管道与所述脱硫剂喷洒管线连接。脱硫剂一般选择的是碱液，碱液循环进入到脱硫塔与从脱硫塔底部进入的气相逆向接触，喷洒吸收以实现脱硫，脱硫之后的碱液再返回到脱硫剂储罐中，当脱硫剂储罐中的碱液循环使用过程中污染比较严重的情况下，停车进行更换。
优选地，所述脱硫剂喷洒管线为三排，每排所述脱硫剂喷洒管线相互平行设置。通过三排喷射管线的铺设，可以提高脱硫剂对气相中的硫化氢的吸收效果。
优选地，本发明还可以在加氢反应器内设置微界面发生器，所述微界面发生器设置在所述液体喷射器的正下方，将微界面发生器与液体喷射器结合使用，以提高两者之间互相协同配合的效果。
优选地，所述微界面发生器的个数为单个，且其具体类型最好为气动式微界面发生器，因为气动式类型相对成本低，容易安装。
优选地，在所述加氢反应器的侧壁上设置有用于进入氢气的进气口，所述进气口与所述脱硫塔的侧壁连接用于将纯化后的氢气循环利用，所述进气口通过管道与微界面发生器连接。从精制加氢反应器出来的反应产物经过液相产品回收后，气相送往脱硫塔进行脱硫，气相中的成分主要为硫化氢和氢气，通过在脱硫塔中将硫化氢吸收后，氢气则从与脱硫塔连接的进气口进入到微界面发生器中，与从原料进口进来的油品接触进行分散破碎。
加氢反应器内的微界面发生器将空气破碎成微米尺度的微气泡，并将微气泡释放到内部，以增大反应过程中原料之间的相界传质面积，使得两相充分接触，提高液相中的溶解气体的浓度，提高效率，缩短反应时间。
本领域所属技术人员可以理解的是，本发明所采用的微界面发生器在本发明人在先专利中已有体现，如申请号CN201610641119.6、CN201610641251.7、CN201710766435.0、CN106187660、CN105903425A、CN109437390A、CN205833127U及CN207581700U的专利。在先专利CN201610641119.6中详细介绍了微米气泡发生器(即微界面发生器)的具体产品结构和工作原理，该申请文件中记载了“微米气泡发生器包括本体和二次破碎件、本体内具有空腔，本体上设有与空腔连通的进口，空腔的相对的第一端和第二端均敞开，其中空腔的横截面积从空腔的中部向空腔的第一端和第二端减小；二次破碎件设在空腔的第一端和第二端中的至少一个处，二次破碎件的一部分设在空腔内，二次 破碎件与空腔两端敞开的通孔之间形成一个环形通道。微米气泡发生器还包括进气管和进液管。”从该申请文件中公开的具体结构可以知晓其具体工作原理为：液体通过进液管切向进入微米气泡发生器内，超高速旋转并切割气体，使气体气泡破碎成微米级别的微气泡，从而提高液相与气相之间的传质面积，而且该专利中的微米气泡发生器属于气动式微界面发生器。
另外，在先专利201610641251.7中有记载一次气泡破碎器具有循环液进口、循环气进口和气液混合物出口，二次气泡破碎器则是将进料口与气液混合物出口连通，说明气泡破碎器都是需要气液混合进入，另外从后面的附图中可知，一次气泡破碎器主要是利用循环液作为动力，所以其实一次气泡破碎器属于液动式微界面发生器，二次气泡破碎器是将气液混合物同时通入到椭圆形的旋转球中进行旋转，从而在旋转的过程中实现气泡破碎，所以二次气泡破碎器实际上是属于气液联动式微界面发生器。其实，无论是液动式微界面发生器，还是气液联动式微界面发生器，都属于微界面发生器的一种具体形式，然而本发明所采用的微界面发生器并不局限于上述几种形式，在先专利中所记载的气泡破碎器的具体结构只是本发明微界面发生器可采用的其中一种形式而已。此外，在先专利201710766435.0中记载到“气泡破碎器的原理就是高速射流以达到气体相互碰撞”，并且也阐述了其可以用于微界面强化反应器，验证本身气泡破碎器与微界面发生器之间的关联性；而且在先专利CN106187660中对于气泡破碎器的具体结构也有相关的记载，具体见说明书中第[0031]-[0041]段，以及附图部分，其对气泡破碎器S-2的具体工作原理有详细的阐述，气泡破碎器顶部是液相进口，侧面是气相进口，通过从顶部进来的液相提供卷吸动力，从而达到粉碎成超细气泡的效果，附图中也可见气泡破碎器呈锥形的结构，上部的直径比下部的直径要大，也是为了液相能够更好的提供卷吸动力。
由于在先专利申请的初期，微界面发生器才刚研发出来，所以早期命名为微米气泡发生器(CN201610641119.6)、气泡破碎器(201710766435.0)等，随着不断技术改进，后期更名为微界面发生器，现在本发明中的微界面发生器 相当于之前的微米气泡发生器、气泡破碎器等，只是名称不一样。
综上所述，本发明的微界面发生器属于现有技术，虽然有的微界面发生器属于气动式微界面发生器类型，有的微界面发生器属于液动式微界面发生器类型，还有的属于气液联动式微界面发生器类型，但是类型之间的差别主要是根据具体工况的不同进行选择，另外关于微界面发生器与反应器、以及其他设备的连接，包括连接结构、连接位置，根据微界面发生器的结构而定，此不作限定。
与现有技术相比，本发明的有益效果在于：
(1)本发明的加氢强化微界面系统通过在加氢反应器内设置液体喷射器，一方面液体喷射器可将清洗加氢反应器的水高效破碎成微米级液滴，并通过喷射器冲撞加氢反应器上方取代人工进行清洗，此外还可将液体喷射器应用于原料进入加氢反应器的喷射，从而达到提高反应传质的效果；
(2)本发明的加氢强化微界面系统可以实现将液体喷射器与微界面发生器进行协同合作，以使微界面发生器将空气破碎成微米尺度的微气泡，并将微气泡释放到内部，以增大反应过程中原料之间的相界传质面积，使得两相充分接触，提高液相中的溶解气体的浓度，提高效率，缩短反应时间。
附图说明
通过阅读下文优选实施方式的详细描述，各种其他的优点和益处对于本领域普通技术人员将变得清楚明了。附图仅用于示出优选实施方式的目的，而并不认为是对本发明的限制。而且在整个附图中，用相同的参考符号表示相同的部件。在附图中：
图1为本发明实施例提供的加氢强化微界面系统的结构示意图；
图2为本发明实施例提供的加氢强化微界面系统的网面的结构示意图。
附图说明：
10-加氢反应器；                     101-进液口；
102-出液口；                        103-液体喷射器；
1031-喷射口；                       1032-网面；
104-搅拌桨；                        105-微界面发生器；
106-进气口；                        107-原料进口；
20-精制加氢反应器；                 30-脱硫塔；
40-脱硫剂储罐。
具体实施方式
下面将结合附图和具体实施方式对本发明的技术方案进行清楚、完整地描述，但是本领域技术人员将会理解，下列所描述的实施例是本发明一部分实施例，而不是全部的实施例，仅用于说明本发明，而不应视为限制本发明的范围。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。实施例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。
在本发明的描述中，需要说明的是，术语“中心”、“上”、“下”、“左”、“右”、“竖直”、“水平”、“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本发明和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本发明的限制。此外，术语“第一”、“第二”、“第三”仅用于描述目的，而不能理解为指示或暗示相对重要性。
在本发明的描述中，需要说明的是，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是机械连接，也可以是电连接；可以是直接相连， 也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域的普通技术人员而言，可以具体情况理解上述术语在本发明中的具体含义。
为了更加清晰的对本发明中的技术方案进行阐述，下面以具体实施例的形式进行说明。
实施例
参阅图1所示，为本发明实施例的加氢强化微界面系统，其主要包括加氢反应器10、精制加氢反应器20、脱硫塔30以及脱硫剂储罐40；加氢反应器10内上部以及侧壁均设置有液体喷射器103，同时加氢反应器内还设置有微界面发生器105，微界面发生器105正好设置在液体喷射器103的正下方，加氢反应器10的侧壁设置有进液口101以及产物出口，还设置有用于进入氢气的进气口106，在加氢反应器10的侧壁上还设置有用于进入油品的原料进口107，原料进口107设置在加氢反应器10侧壁靠下的位置，这样原料进口107比较靠近进气口106，进来的油品能够与氢气发生接触，提高氢气的破碎分散效果。
位于上部的液体喷射器103与进液口101通过管道连接，位于侧壁的液体喷射器103与原料进口107通过管道连接，液体喷射器103的底部为平面，顶面呈半圆形弧面，所述半圆形弧面上依次排布有若干个喷射口1031，位于上部的所述喷射口1031的喷射方向朝向加氢反应器10顶部，位于侧壁的喷射口1031的方向朝向加氢反应器的对侧壁，进液口101通过管道与液体喷射器103的底部连接，最优是通过与液体喷射器103的底部中心连接，通过将进入液体喷射器103的液体破碎为直径为微米级的微液滴，从表面凸起的喷射口1031喷出，以冲撞加氢反应器顶部进行高效的清洗。为了提高喷射效果，喷射口1031内铺设有均布多个微孔的网面1032，网面1032的个数不限，目的是为了使液体呈雾状喷射出去，提高传质效果，网面1032的结构具体参见图2。
微界面发生器105的个数单个，进气口106与脱硫塔30的侧壁连接用于 将纯化后的氢气重新送回到加氢反应器中进行循环利用，并且进气口106通过管道与相对应的微界面发生器105连接。
加氢反应器10的底部设置有出液口102，用于将堆积在加氢反应器10底部的物料出料。加氢反应器10的底部两侧平整，中心位置向上凸起呈平面，在加氢反应器10底部的两侧平整位置分别设置有所述出液口102，出液口102用于排出废液，加氢反应器10内底部中心凸起平面设置有搅拌桨104以起到加速排料的作用，叶片的方向朝上，以用于加氢反应器10底部冲洗与排液时的搅拌，转速可以无级调节。优选地搅拌桨的个数为两个，并排设置在加氢反应器10底部凸起平面处。
此外，在脱硫塔30的旁侧设置有脱硫剂储罐40，脱硫剂储罐40与脱硫塔30的侧壁下部通过管道连接，脱硫剂储罐40的顶部通过管道与脱硫剂喷洒管线连接，脱硫剂喷洒管线为三排，每排脱硫剂喷洒管线相互平行设置。
该实施例还包括PLC(或DCS，PLC和DCS)控制系统：与加氢反应器10的传感器相连，用于智能化控制工艺操作与参数，实现了对生产进行远程控制，符合生产的智能化。
本发明实施例的加氢强化微界面系统的工作过程如下：
(1)清洗：在加氢反应器10上方的清洗水通过进液口101输送到液体喷射器103内部并通过弧面上的喷射口1031将水喷淋出来，经网面1032高效破碎成微米级(1μm≤d<1mm)液滴后从液体喷射器103表面凸起的喷射口1031喷出，冲撞加氢反应器10的顶部并对上方进行清洗。清洗后的液滴在罐底形成液位，当液位上升到加氢反应器10中部时，关闭上方输水阀门，打开底部的搅拌桨104到200rpm。由于搅拌桨104叶片的安装方向向下，会将叶片上方的液体抽往下方两侧，并在搅拌桨104两侧形成漩涡，对加氢反应器10下部两侧进行冲刷清洗。同时打开下方的水路，输入的水流在搅拌桨104的作用下对加氢反应器侧壁进行清洗，冲刷30min后关闭输水阀门，调小转速到100rpm/min，并通过加氢反应器10下端两侧的出液口102将水排出，关闭出 液口102，调小转速到50rpm/min。
(2)工作：氢气与从侧壁的液体喷射器出来的直馏柴油先在加氢反应器10内进行加氢反应，进行加氢反应之前，将氢气通入位于加氢反应器10内部的微界面发生器105中，进行分散破碎后使得气体形成微气泡，更有利于反应高效的进行，加氢反应后，反应产物通过管道送入精制加氢反应器20中进行深度加氢反应。进行深度加氢反应后的反应产物经过分离后，液相回收气相进入脱硫塔30中，实现对气相中硫化氢的吸收，吸收完净化的氢气重新返回到加氢反应器中进行利用。
上述加氢强化微界面系统工作过程中的操作以及工艺参数完全由PLC(或DCS，PLC和DCS)的控制系统控制，控制系统与加氢反应器10上各传感器相连接，实现自动化智能化控制，节约人力成本。
上述加氢反应的压力2-8MPa，所述加氢反应的温度为250-320℃。最优选地，加氢反应的压力为3.5MPa，加氢反应的温度为300℃。
精制加氢反应的压力2-8MPa，所述精制加氢反应的温度为250-320℃。最优选地，精制加氢反应的压力为3.5MPa，精制加氢反应的温度为300℃。
加氢反应与精制加氢反应均采用的催化剂为Mo-Ni型催化剂，加氢反应器10与精制加氢反应器20内的催化剂用量体积比可以为(1:12)-(1:15)，较优地为1:13。
总之，本发明的方案通过液体喷射器与微界面发生器的协同配合，不仅实现了对液相的分散破碎，也实现了对气相的分散破碎，这样通过将各个相态的物质均破碎成微米颗粒，从而更能提高体系的传质效果。
在上述实施例中，泵体的个数并没有具体要求，可根据需要在相应的位置设置。
最后应说明的是：以上各实施例仅用以说明本发明的技术方案，而非对其限制；尽管参照前述各实施例对本发明进行了详细的说明，本领域的普通技术人员应当理解：其依然可以对前述各实施例所记载的技术方案进行修改，或者 对其中部分或者全部技术特征进行等同替换；而这些修改或者替换，并不使相应技术方案的本质脱离本发明各实施例技术方案的范围。

Claims (7)

  1. 一种加氢强化微界面系统，其特征在于，包括：加氢反应器；
    所述加氢反应器的底面中间区域向上凸起呈平面，在所述加氢反应器底面凸起平面的两侧平整部分别设置有出液口，所述加氢反应器的侧壁上设置有进液口以及产物出口，所述加氢反应器的侧壁设置有用于进入油品的原料进口，所述原料进口设置在所述加氢反应器侧壁靠下的位置；
    所述加氢反应器内上部以及侧壁均设置有液体喷射器，所述液体喷射器的底部为平面，顶部呈半圆形弧面，所述半圆形弧面上依次排布有若干个喷射口，位于上部的液体喷射器的所述喷射口的喷射方向朝向加氢反应器的顶部，位于侧壁的液体喷射器的所述喷射口的喷射方向朝向加氢反应器的对侧壁，所述进液口通过管道与所述液体喷射器的底部连接，所述原料进口与所述液体喷射器的底部连接；
    所述产物出口连接精制加氢反应器进行深度加氢反应，从所述精制加氢反应器底部出来的反应产物分离出的气相进入脱硫塔中，以实现对气相中硫化氢的吸收。
  2. 根据权利要求1所述的加氢强化微界面系统，其特征在于，所述加氢反应器内设置有微界面发生器，所述微界面发生器设置在所述液体喷射器的正下方。
  3. 根据权利要求2所述的加氢强化微界面系统，其特征在于，在所述加氢反应器的侧壁上设置有用于进入氢气的进气口，所述进气口与所述脱硫塔的侧壁连接用于将纯化后的氢气循环利用，所述进气口通过管道与微界面发生器连接。
  4. 根据权利要求1所述的加氢强化微界面系统，其特征在于，所述加氢反应器内底部向上凸起处设置有搅拌桨以起到加速排料的作用。
  5. 根据权利要求4所述的加氢强化微界面系统，其特征在于，所述搅拌桨的数量为两个，并排设置在所述加氢反应器底部凸起平面处。
  6. 根据权利要求1-5任一项所述的加氢强化微界面系统，其特征在于，所述脱硫塔的旁侧设置有脱硫剂储罐，所述脱硫剂储罐与所述脱硫塔的侧壁下部通过管道连接，所述脱硫剂储罐的顶部通过管道与所述脱硫剂喷洒管线连接。
  7. 根据权利要求6所述的加氢强化微界面系统，其特征在于，所述脱硫剂喷洒管线为三排，每排所述脱硫剂喷洒管线相互平行设置。
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