Efficient continuous oily sludge pyrolysis device and method

Abstract

The invention provides an efficient continuous oily sludge pyrolysis device and method, the efficient continuous oily sludge pyrolysis device comprises a pyrolysis assembly (10), and the pyrolysis assembly (10) comprises a first-stage pyrolysis reactor (100), a second-stage pyrolysis reactor (101) and a third-stage pyrolysis reactor (102) which are sequentially communicated from top to bottom. By introducing the continuous pyrolysis design, the downtime is shortened, the treatment efficiency of the oily sludge is remarkably improved, and the requirement for large-scale oily sludge treatment is met; the design of bottom combustion gas heating and top feeding is adopted for the pyrolysis reactor, so that a high-low temperature area is effectively formed, the pyrolysis temperature gradient is enhanced, rapid decomposition of the oily sludge is promoted, the heat utilization rate is increased, and the heat loss is reduced.

Description

Technical Field

[0001] The invention relates to the field of solid waste organic matter treatment, and in particular to a high-efficiency continuous oily sludge pyrolysis device and method. Background Art

[0002] In the process of oil field exploitation, oil refining, transportation, use, storage and other links, a large amount of oily sludge will inevitably be produced, and its improper disposal poses a serious threat to the environment and public health. At present, my country classifies it as HW08 hazardous waste. However, the high content of organic hydrocarbons in oily sludge makes it have considerable potential for resource utilization. Oily sludge is mainly composed of crude oil, oil-contaminated solids (such as sand and fine clay) and water, but the additives added in the oil production process significantly increase the viscosity and density of oily sludge, resulting in the oily sludge mainly existing in an emulsified form. Surfactants adhering to oily sludge particles are prone to produce amphiphilic particles, and their strong adhesion makes it challenging to separate oil from solids using traditional mechanical or chemical methods. With the increasingly stringent energy crisis and environmental regulations, how to safely dispose of oily sludge and effectively recover the oil resources in it has become an urgent problem to be solved.

[0003] Traditional centrifugal separation technology uses centrifugal force to quickly and effectively separate oil, water and solid components. However, the centrifugal separation efficiency is significantly affected by the physical properties of the oil, such as viscosity and specific gravity. For some highly emulsified or fine suspended oil sludge, the separation effect is not good. Solvent extraction can use extractants to extract petroleum substances from oily sludge, but this method is still in the development stage, and the extractant is expensive and the processing cost is high. Pyrolysis of oily sludge is a technology that effectively utilizes organic matter in oily sludge, which can be converted into usable oil gas and carbon slag, thereby recovering a higher proportion of oil resources. The three-phase products (gas, liquid, solid) generated during the pyrolysis process can be further utilized to increase economic benefits. At the same time, the pyrolysis process reduces the emission of harmful substances and is more environmentally friendly than traditional incineration methods. However, the traditional pyrolysis process usually requires continuous high temperature, and there are problems such as low thermal utilization and large heat loss, which increases operating costs. Summary of the invention

[0004] In view of the above-mentioned shortcomings of the prior art, the object of the present invention is to provide a high-efficiency continuous oily sludge pyrolysis device and method for solving the problem of low heat utilization rate of oily sludge pyrolysis in the prior art.

[0005] To achieve the above objectives and other related objectives, the present invention is achieved through the following technical solutions.

[0006] The invention provides a high-efficiency continuous oily sludge pyrolysis device, comprising a pyrolysis component, wherein the pyrolysis component comprises a primary pyrolysis reactor, a secondary pyrolysis reactor and a tertiary pyrolysis reactor which are sequentially connected and arranged from top to bottom.

[0007] Preferably, the primary pyrolysis reactor comprises a first horizontal screw propeller for conveying materials, the secondary pyrolysis reactor comprises a second horizontal screw propeller for conveying materials, and the tertiary pyrolysis reactor comprises a third horizontal screw propeller for conveying materials.

[0008] More preferably, a gap d between the first horizontal screw propeller and the inner wall of the reaction chamber of the primary pyrolysis reactor is 20 to 25 mm.

[0009] More preferably, a gap d between the second horizontal screw propeller and the inner wall of the reaction chamber of the secondary pyrolysis reactor is 20 to 25 mm.

[0010] More preferably, a gap d between the third horizontal screw propeller and the inner wall of the reaction chamber of the three-stage pyrolysis reactor is 20 to 25 mm.

[0011] Preferably, the primary pyrolysis reactor includes a first fuel gas chamber for providing reaction heat supply, the secondary pyrolysis reactor includes a second fuel gas chamber for providing reaction heat supply, and the tertiary pyrolysis reactor includes a third fuel gas chamber for providing reaction heat supply.

[0012] Preferably, the pyrolysis component includes an oily sludge pipeline, a combustion gas pipeline and a pyrolysis gas pipeline; the oily sludge pipeline, the combustion gas pipeline and the pyrolysis gas pipeline are respectively connected to the primary pyrolysis reactor, the secondary pyrolysis reactor and the tertiary pyrolysis reactor in sequence, and the oily sludge pipeline is used to allow the oily sludge to react step by step from top to bottom; the combustion gas pipeline is used to supply the combustion gas step by step from bottom to top; the pyrolysis gas pipeline is used to transport the pyrolysis gas step by step from bottom to top to participate in the pyrolysis reaction.

[0013] More preferably, the combustion gas pipeline is connected to the first gas chamber, the second gas chamber and the third gas chamber in sequence.

[0014] More preferably, the input ends of the oily sludge pipelines corresponding to the primary pyrolysis reactor, the secondary pyrolysis reactor and the tertiary pyrolysis reactor and the gas inlet ends of the corresponding pyrolysis gas pipelines are arranged at the same end of the corresponding pyrolysis reactors, so that the oily sludge and pyrolysis gas are transported along the same material conveying direction in the same-stage pyrolysis reactor.

[0015] Further preferably, the input ends of the oily sludge pipelines corresponding to the primary pyrolysis reactor, the secondary pyrolysis reactor and the tertiary pyrolysis reactor and the gas inlet ends of the corresponding combustion gas pipelines are arranged at the same end of the corresponding pyrolysis reactors, so that the oily sludge and the combustion gas are transported along the same material conveying direction in the same-stage pyrolysis reactor.

[0016] More preferably, the pyrolysis component further comprises a combustion gas and tail gas treatment unit, and the combustion gas and tail gas treatment unit is connected to the combustion gas exhaust end of the primary pyrolysis reactor through a pipeline.

[0017] More preferably, a flow control regulating valve is provided on the combustion gas pipeline.

[0018] More preferably, a burner is provided at the air inlet end of the combustion gas pipeline 106 .

[0019] Preferably, the primary pyrolysis reactor, the secondary pyrolysis reactor and the tertiary pyrolysis reactor are each provided with a pressure sensor and / or a temperature sensor.

[0020] More preferably, the pyrolysis component also includes a pyrolysis process controller, which is connected to the pressure sensor and / or temperature sensor signal, and is used to control the combustion gas supply of the pyrolysis component based on the obtained temperature signal, and determine whether to issue a safety warning based on the obtained pressure signal.

[0021] Preferably, the high-efficiency continuous oily sludge pyrolysis device also includes a pretreatment component; the pretreatment component is arranged upstream of the pyrolysis component, and is used to pretreat the oily sludge to be pyrolyzed and then transport it to the pyrolysis component; the pretreatment component includes a pretreatment unit, a conveying unit and an oily sludge pipeline in sequence along the process direction.

[0022] More preferably, the pretreatment unit comprises a filter press and a pulverizer in sequence along the process direction.

[0023] Further preferably, the feed end of the filter press is connected to an oily sludge storage tank, a feed pump and a feed flow meter.

[0024] More preferably, the conveying unit comprises a conveyor belt, a bucket elevator, a silo and a screw feeder in sequence along the process direction, and the screw feeder is connected to the oily sludge pipeline.

[0025] Preferably, the oily sludge pyrolysis device also includes a pyrolysis gas recovery component, which is connected to the pyrolysis gas exhaust end of the pyrolysis component through a pipeline, and is used for post-processing the pyrolysis gas exhaust gas of the pyrolysis component to obtain light oil and heavy oil respectively; along the process direction, the pyrolysis gas recovery component includes a pyrolysis gas condenser, a centrifuge and an oil phase fractionation tower which are connected in sequence.

[0026] More preferably, the centrifuge is connected to the feed inlet of the oil phase fractionation tower through an oil phase pipeline.

[0027] Further preferably, the oil phase pipeline is also provided with an oil storage tank and / or an oil pump and / or a flow meter.

[0028] More preferably, the light oil discharge end of the oil phase fractionation tower (305) is also connected to a fractionation condenser and a gas-liquid separator in sequence through pipelines.

[0029] Further preferably, the gas-liquid separator is connected to the tail gas absorption tower via a gas pipeline.

[0030] More preferably, the bottom of the oil phase fractionation tower is further provided with a fractionation reboiler for further fractionating the bottom oil phase of the oil phase fractionation tower to obtain heavy oil and secondary light oil for reflux to the oil phase fractionation tower.

[0031] More preferably, the centrifuge is also connected to a water phase pipeline and a water phase storage component.

[0032] More preferably, the centrifuge is further connected to a tail gas absorption tower via a gas phase pipeline.

[0033] Further preferably, an air pump is provided on the gas phase pipeline.

[0034] The invention also discloses a method for pyrolyzing oily sludge using the efficient continuous oily sludge pyrolysis device as described above.

[0035] Preferably, the reaction temperature of the primary pyrolysis reactor is 350-450° C. The primary pyrolysis reactor is used to evaporate and decompose the water and light volatile components in the oily sludge.

[0036] Preferably, the reaction pressure of the primary pyrolysis reactor is 0.05-0.15 MPa, such as 0.05-0.1 MPa, 0.1-0.15 MPa.

[0037] Preferably, the heating rate of the primary pyrolysis reactor is 5-20°C / min.

[0038] Preferably, the relative humidity of the primary pyrolysis reactor during the reaction is 50-80% RH.

[0039] Preferably, the reaction time of the primary pyrolysis reactor is 0.5 to 1 h.

[0040] Preferably, the reaction temperature of the secondary pyrolysis reactor is 450-550° C. The secondary pyrolysis reactor is used to crack the heavy components in the oily sludge and generate more pyrolysis gas and oil.

[0041] Preferably, the reaction pressure of the secondary pyrolysis reactor is 0.05-0.15 MPa, such as 0.05-0.1 MPa, 0.1-0.15 MPa.

[0042] Preferably, the heating rate of the secondary pyrolysis reactor is 5-20°C / min.

[0043] Preferably, the relative humidity of the secondary pyrolysis reactor during the reaction is 50-80% RH.

[0044] Preferably, the reaction time of the secondary pyrolysis reactor is 0.5 to 1 h.

[0045] Preferably, the reaction temperature of the three-stage pyrolysis reactor is 550-700° C. The three-stage pyrolysis reactor is used to further crack the heavy components in the oily sludge, thereby increasing the output of pyrolysis gas and oil.

[0046] Preferably, the reaction pressure of the three-stage pyrolysis reactor is 0.05-0.15 MPa, such as 0.05-0.1 MPa, 0.1-0.15 MPa.

[0047] Preferably, the heating rate of the three-stage pyrolysis reactor is 5-20°C / min. The pyrolysis efficiency and product yield are optimized by controlling the reaction pressure and heating rate of the pyrolysis reactor.

[0048] Preferably, the relative humidity of the three-stage pyrolysis reactor during the reaction is 50-80% RH. During the pyrolysis process, if the humidity is too high or too low, the pyrolysis efficiency will be affected.

[0049] Preferably, the reaction time of the three-stage pyrolysis reactor is 1 to 2 hours. Preferably, the oily sludge undergoes a primary pyrolysis reaction in the primary pyrolysis reactor, and the sludge outlet stream of the primary pyrolysis reactor after the primary pyrolysis reaction enters the secondary pyrolysis reactor for a secondary pyrolysis reaction, and the sludge outlet stream of the secondary pyrolysis reactor after the secondary pyrolysis reaction enters the three-stage pyrolysis reactor for a three-stage pyrolysis reaction.

[0050] More preferably, the reaction time of the primary pyrolysis reaction is 0.5 to 1 h.

[0051] More preferably, the reaction time of the secondary pyrolysis reaction is 0.5 to 1 h.

[0052] More preferably, the reaction time of the three-stage pyrolysis reaction is 1 to 2 hours.

[0053] More preferably, the reaction atmosphere of the primary pyrolysis reaction, the secondary pyrolysis reaction and the tertiary pyrolysis reaction are all nitrogen atmospheres, and the nitrogen flow rate is 5 to 100 L / min.

[0054] Preferably, the combustion gas enters the second combustion chamber and the first combustion chamber in sequence from the third combustion chamber, and the combustion gas provides heat for the pyrolysis reaction.

[0055] Preferably, the combustion gas includes natural gas and air in a volume ratio of 1:(10-15).

[0056] Preferably, the pyrolysis gas enters the secondary pyrolysis reactor and the primary pyrolysis reactor in sequence from the tertiary pyrolysis reactor.

[0057] Preferably, an intelligent control unit is also provided in the pyrolysis component, and the intelligent control unit is connected to the pressure sensor and / or the temperature sensor and / or the humidity sensor, and is used to receive data from the pressure sensor and / or the temperature sensor and / or the humidity sensor.

[0058] More preferably, the intelligent control unit comprises an alarm module, and the intelligent control unit is signal-connected to the alarm module for triggering a safety warning according to a control instruction.

[0059] Further preferably, the intelligent control unit includes a pressure calculation module, which is used to receive a pressure setting value and determine whether the pressure monitored in real time by the pressure sensor is higher than a threshold value. If so, the intelligent control unit sends a control instruction to the alarm module to send an alarm message of pipeline blockage. Specifically, the threshold value is set to 0.1MPa.

[0060] More preferably, the intelligent control unit is connected to the flow control regulating valve signal to adjust the flow rate of the flow control regulating valve according to a control instruction.

[0061] Further preferably, the intelligent control unit includes a temperature calculation module, which is used to receive a minimum threshold and a maximum threshold, and determine whether the temperature monitored in real time by the temperature sensor of the pyrolysis reactor is higher than the maximum threshold. If so, the intelligent control system sends a control instruction to the flow control regulating valve to reduce the flow; and determine whether the temperature monitored in real time by the temperature sensor of the pyrolysis reactor is lower than the minimum threshold. If so, the intelligent control system sends a control instruction to the flow control regulating valve to increase the flow. The temperature threshold of the pyrolysis reactor is ±10°C of the set value.

[0062] Further preferably, the intelligent control unit includes a humidity calculation module, which is used to receive a minimum threshold and a maximum threshold, and determine whether the humidity monitored in real time by the humidity sensor is higher than the maximum threshold. If so, the intelligent control unit sends a control instruction to the flow control regulating valve to increase the flow; and determines whether the humidity monitored in real time by the temperature sensor is lower than the minimum threshold. If so, the intelligent control system sends a control instruction to the flow control regulating valve to reduce the flow. The threshold of humidity is ±10%RH of the set value. The pyrolysis efficiency is improved by controlling the humidity during the pyrolysis reaction.

[0063] Preferably, the water content of the oily sludge treated by the filter press 201 is 20-30wt%.

[0064] Preferably, the particle size of the oily sludge processed by the pulverizer 203 is no more than 5 mm.

[0065] Preferably, the combustion gas escaping from the first gas chamber is discharged after being treated.

[0066] Preferably, the pyrolysis gas escaping from the primary pyrolysis reactor is recycled.

[0067] More preferably, the pyrolysis gas is cooled, separated from oil and water, and fractionated to obtain light oil and heavy oil.

[0068] More preferably, the light component after distillation is cooled and separated into gas and liquid to obtain light oil; preferably, the bottom oil phase remaining after distillation and further distillation is heavy oil.

[0069] Preferably, the oil content of the oily sludge after pyrolysis treatment by the oily sludge pyrolysis device is less than 3‰.

[0070] Preferably, the weight of the oily sludge is reduced by at least 70wt% after being pyrolyzed by the oily sludge pyrolysis device.

[0071] Compared with the prior art, the present invention has the following beneficial effects:

[0072] (1) By introducing a continuous pyrolysis design, downtime is reduced, the treatment efficiency of oily sludge is significantly improved, and the needs of large-scale oily sludge treatment are met;

[0073] (2) By adopting the design of bottom combustion gas heating and top feeding in the pyrolysis reactor, high and low temperature areas are effectively formed, the pyrolysis temperature gradient is enhanced, the rapid decomposition of oily sludge is promoted, the heat utilization rate is improved and the heat loss is reduced;

[0074] (3) By mixing the pyrolysis gas generated during the pyrolysis process with the incompletely pyrolyzed oily sludge, the decomposition and conversion of the oily sludge is further promoted, thereby generating more usable gas and liquid oil products and improving the overall resource utilization rate;

[0075] (4) By using a primary pyrolysis reactor, a secondary pyrolysis reactor, and a tertiary pyrolysis reactor arranged from top to bottom, not only the oily sludge is transported to the next pyrolysis reactor by gravity, thus reducing energy consumption, but also the pyrolysis gas is facilitated to flow from the tertiary pyrolysis reactor to the primary pyrolysis reactor;

[0076] (5) After fractionation and purification, the pyrolysis gas can effectively recover light hydrocarbons and heavy hydrocarbons, realize the secondary utilization of resources, and thus achieve the multiple goals of maximizing resource utilization, reducing volume, and harmless treatment of oily sludge.

[0077] (6) The gap d between the inner cavity of the pyrolysis reactor and the screw propeller is designed to be small. In the process of pushing the oily sludge forward, the oily sludge forms a mud cake in the cavity, which increases the contact area between the pyrolysis gas and the oily sludge, and avoids the oily sludge from easily agglomerating during the pushing process, resulting in incomplete pyrolysis of the local oily sludge;

[0078] (7) The screw propeller is a huge roller, and the roller cavity is filled with inert gas or evacuated to isolate heat transfer. Compared with the traditional screw propeller roller, it avoids the local deformation of the roller caused by long-term operation in a high-temperature environment;

[0079] (8) The overall device adopts a longitudinal layout, which significantly reduces construction investment and land costs. At the same time, compared with the general long-body single rotary furnace, the rotating shaft of the screw propeller is shorter and the operating torque is significantly reduced, so that the propeller motor can use an ordinary three-phase asynchronous motor, achieving lower power consumption. In addition, this design also reduces the maintenance cost of the rotating shaft, further improving the economy and efficiency of the system. BRIEF DESCRIPTION OF THE DRAWINGS

[0080] Figure 1 Shown is a schematic structural diagram of the pyrolysis assembly of the present invention.

[0081] Figure 2 Shown is a schematic structural diagram of the pretreatment component of the present invention.

[0082] Figure 3 Shown is a schematic structural diagram of the pyrolysis gas recovery component of the present invention.

[0083] Figure 4 Shown is a schematic structural diagram of the high-efficiency continuous oily sludge pyrolysis device of the present invention.

[0084] Description of reference numerals:

[0085]

[0086] DETAILED DESCRIPTION

[0087] The following is a description of the implementation of the present invention by means of specific embodiments. Those skilled in the art can easily understand other advantages and effects of the present invention from the contents disclosed in this specification.

[0088] Before further describing the specific embodiments of the present invention, it should be understood that the scope of protection of the present invention is not limited to the specific embodiments described below; it should also be understood that the terms used in the examples of the present invention are intended to describe specific embodiments, rather than to limit the scope of protection of the present invention. The test methods in the following examples without specifying specific conditions are generally carried out under conventional conditions or under conditions recommended by the manufacturers.

[0089] When the embodiments give numerical ranges, it should be understood that, unless otherwise specified in the present invention, both endpoints of each numerical range and any numerical value between the two endpoints can be selected. Unless otherwise defined, all technical and scientific terms used in the present invention have the same meaning as those generally understood by those skilled in the art. In addition to the specific methods, equipment, and materials used in the embodiments, according to the grasp of the prior art by those skilled in the art and the record of the present invention, any methods, equipment, and materials of the prior art similar or equivalent to the methods, equipment, and materials described in the embodiments of the present invention can also be used to realize the present invention.

[0090] Example 1

[0091] This embodiment provides a specific high-efficiency continuous oily sludge pyrolysis device, the schematic diagram of the device is as follows Figures 1 to 3 As shown:

[0092] In a specific Figure 1In the illustrated embodiment, the high-efficiency continuous oily sludge pyrolysis device comprises a pyrolysis assembly 10, and the pyrolysis assembly 10 comprises a primary pyrolysis reactor 100, a secondary pyrolysis reactor 101 and a tertiary pyrolysis reactor 102 which are sequentially connected and arranged from top to bottom. The oily sludge undergoes a primary pyrolysis reaction in the primary pyrolysis reactor 100, and the sludge outlet stream of the primary pyrolysis reactor 100 after the primary pyrolysis reaction enters the secondary pyrolysis reactor 101 for a secondary pyrolysis reaction, and the sludge outlet stream of the secondary pyrolysis reactor 101 after the secondary pyrolysis reaction enters the tertiary pyrolysis reactor 102 for a tertiary pyrolysis reaction. By introducing a three-stage continuous pyrolysis design and combining it with a top-down setting, downtime is reduced, the treatment efficiency of oily sludge is significantly improved, and the needs of large-scale oily sludge treatment are met; and in actual pyrolysis operations, a pyrolysis temperature gradient can be formed in the first-stage pyrolysis reactor 100, the second-stage pyrolysis reactor 101 and the third-stage pyrolysis reactor 102 that are sequentially connected from top to bottom, thereby promoting the rapid decomposition of oily sludge, improving the recovery rate of pyrolysis oil, improving heat utilization, reducing heat loss, reducing energy consumption, and achieving a reduction effect.

[0093] In a Figure 1 In the specific embodiment shown, the primary pyrolysis reactor 100 includes a first horizontal screw propeller for conveying materials, the secondary pyrolysis reactor 101 includes a second horizontal screw propeller for conveying materials, and the tertiary pyrolysis reactor 102 includes a third horizontal screw propeller for conveying materials. This horizontal structure is used to make the entire device more compact, and the screw propulsion provides power for mass transfer and heat transfer.

[0094] In a more specific embodiment, the gap between the first horizontal screw propeller and the inner wall of the reaction chamber of the primary pyrolysis reactor 100 is 20-25 mm.

[0095] In a more specific embodiment, the gap between the second horizontal screw propeller and the inner wall of the reaction chamber of the secondary pyrolysis reactor 100 is 20-25 mm.

[0096] In a more specific embodiment, the gap between the third horizontal screw propeller and the inner wall of the reaction chamber of the three-stage pyrolysis reactor 100 is 20-25 mm.

[0097] In the present application, the gap d between the inner wall of the reaction cavity of each level of pyrolysis reactor and the spiral propeller is designed to be small (smaller than the prior art, which is generally 30-35 mm). In the process of pushing the oily sludge forward, the oily sludge forms a mud cake in the cavity, which increases the contact area between the pyrolysis gas and the oily sludge, and avoids the oily sludge from easily agglomerating during the pushing process, resulting in incomplete pyrolysis of the local oily sludge. Considering the manufacturing accuracy and manufacturing cost, it can also meet the above-mentioned use requirements of the present application.

[0098] In a Figure 1 In the specific embodiment shown, the primary pyrolysis reactor 100 includes a first gas chamber 1001 for providing reaction heat supply, the secondary pyrolysis reactor 101 includes a second gas chamber 1011 for providing reaction heat supply, and the tertiary pyrolysis reactor 102 includes a third gas chamber 1021 for providing reaction heat supply. The gas chambers in each stage of the pyrolysis reactor are also interconnected.

[0099] In a Figure 1 In the specific embodiment shown, the pyrolysis component 10 includes an oily sludge pipeline 103, a combustion gas pipeline 104 and a pyrolysis gas pipeline 106; the oily sludge pipeline 103, the combustion gas pipeline 104 and the pyrolysis gas pipeline 106 are respectively connected to the primary pyrolysis reactor 100, the secondary pyrolysis reactor 101 and the tertiary pyrolysis reactor 102 in sequence, and the oily sludge pipeline 103 is used to allow the oily sludge to react step by step from top to bottom; the combustion gas pipeline 104 is used to supply the combustion gas step by step from bottom to top; and the pyrolysis gas pipeline 106 is used to transport the pyrolysis gas step by step from bottom to top to participate in the pyrolysis reaction.

[0100] Specific to Figure 1 In the example, the connection method of the oily sludge pipeline 103 is as follows Figure 1 As shown in the pipeline marked with an arrow, it is further described as follows: the top and bottom of the first-stage pyrolysis reactor 100 are respectively provided with a first oil-containing sludge feed port and a first oil-containing sludge discharge port; the top and bottom of the second-stage pyrolysis reactor 101 are respectively provided with a second oil-containing sludge feed port and a second oil-containing sludge discharge port; the top and bottom of the tertiary pyrolysis reactor 102 are respectively provided with a third oil-containing sludge feed port and a third oil-containing sludge discharge port; the first oil-containing sludge discharge port is materially connected with the second oil-containing sludge feed port through one section of the oil-containing sludge pipeline 103; the second oil-containing sludge discharge port is materially connected with the third oil-containing sludge feed port through another section of the oil-containing sludge pipeline 103; the third oil-containing sludge discharge port is connected to another section of the oil-containing sludge pipeline 103 to output carbon slag.

[0101] Specific to Figure 1 In the embodiment, the connection method of the pyrolysis gas pipeline 106 is as follows: Figure 1 As shown in the pipeline marked with three arrows, it is specifically described as follows: the top and bottom of the first-stage pyrolysis reactor 100 are respectively provided with a first pyrolysis gas outlet and a first pyrolysis gas inlet, the top and bottom of the second-stage pyrolysis reactor 101 are respectively provided with a second pyrolysis gas outlet and a second pyrolysis gas inlet, the top and bottom of the tertiary pyrolysis reactor 102 are respectively provided with a third pyrolysis gas outlet and a third pyrolysis gas inlet, the third pyrolysis gas outlet is connected to the second pyrolysis gas inlet through one section of the pyrolysis gas pipeline 106, and the second pyrolysis gas outlet is connected to the first pyrolysis gas inlet through another section of the pyrolysis gas pipeline 106. The pyrolysis gas enters the second-stage pyrolysis reactor 101 and the tertiary pyrolysis reactor 102 in sequence from the tertiary pyrolysis reactor 102. The pyrolysis gas is mixed with the incompletely pyrolyzed oily sludge, and direct contact heat transfer is used to further promote the cracking and decomposition of organic matter in the oily sludge. The pyrolysis gas and the incompletely pyrolyzed oily sludge are co-pyrolyzed to promote the cracking and decomposition of organic matter in the oily sludge. The above method effectively utilizes the waste heat of the pyrolysis gas and improves energy utilization efficiency.

[0102] In a Figure 1 In the more specific embodiment shown, the specific connection method of the combustion gas pipeline 104 is as follows Figure 1 As shown by the double arrows, the specific description is as follows: the combustion gas pipeline 104 sequentially connects the first gas chamber 1001, the second gas chamber 1011 and the third gas chamber 1021 from bottom to top. The pyrolysis gas enters the second gas chamber 1011 of the secondary pyrolysis reactor 101 and the first gas chamber 1001 of the primary pyrolysis reactor 100 from the third gas chamber 1021 of the three-stage pyrolysis reactor 102 in sequence.

[0103] Specific to Figure 1 In the embodiment, the connection mode of the combustion gas pipeline 104 is as follows: the first combustion gas inlet and the first combustion gas outlet are respectively provided at the bottom and the top of the first combustion gas chamber 1001, the second combustion gas inlet and the second combustion gas outlet are respectively provided at the bottom and the top of the second combustion gas chamber 1011, the third combustion gas inlet and the third combustion gas outlet are respectively provided at the bottom and the top of the third combustion gas chamber 1021, the third combustion gas outlet is connected with the second combustion gas inlet through the combustion gas pipeline 104, and the second combustion gas outlet is connected with the first combustion gas inlet through the combustion gas pipeline 104. The combustion gas enters the second combustion gas chamber 1011 and the first combustion gas chamber 1001 in sequence from the third combustion gas chamber 1021 to provide heat for the pyrolysis reaction.

[0104] In a Figure 1In the further specific embodiment shown, the input ends of the oily sludge pipelines 103 corresponding to the primary pyrolysis reactor 100, the secondary pyrolysis reactor 101 and the tertiary pyrolysis reactor 102 and the gas inlet ends of the corresponding combustion gas pipelines 104 are arranged at the same end of the corresponding pyrolysis reactors, so that the oily sludge and the combustion gas are transported along the same material conveying direction in the same-stage pyrolysis reactor.

[0105] In a Figure 1 In the more specific embodiment shown, the input end of the oily sludge pipeline 103 corresponding to the first-stage pyrolysis reactor 100, the second-stage pyrolysis reactor 101 and the third-stage pyrolysis reactor 102 and the air inlet end of the corresponding pyrolysis gas pipeline 106 are arranged at the same end of the corresponding pyrolysis reactor, so that the oily sludge and the pyrolysis gas are transported along the same material transport direction in the same-stage pyrolysis reactor. During the high-temperature pyrolysis process, some liquid oil and gaseous products may undergo secondary reactions in the high-temperature area (such as cracking into non-condensable gas or synthetic coke). In the co-current mode, as the liquid oil and gas products are quickly discharged from the pyrolysis gas exhaust end, they are quickly condensed and separated at a gradually decreasing temperature, which greatly reduces the residence time of the liquid oil and gas products in the high-temperature area, inhibits the secondary cracking reaction in the high-temperature area, and improves the yield and quality of the liquid oil; in addition, the contact time between the pyrolysis gas and the oily sludge is extended, and the pyrolysis reaction efficiency and heat utilization rate are improved.

[0106] In a Figure 1 In the more specific embodiment shown, the pyrolysis assembly 10 further includes a combustion gas tail gas treatment unit 105, and the combustion gas tail gas treatment unit 105 is connected to the combustion gas exhaust end of the primary pyrolysis reactor 100 through a pipeline. The combustion gas escaping from the first combustion chamber 1001 is discharged after being treated. The combustion gas escaping from the first combustion chamber 1001 includes combustion products such as CO2 and SO2, which are treated by the combustion gas tail gas treatment unit 105 and then discharged. In a specific embodiment, the combustion gas tail gas treatment unit 105 adopts a tail gas treatment unit commonly used in the prior art, such as an alkali treatment unit or an adsorbent.

[0107] In a more specific embodiment, a flow control regulating valve is provided on the combustion gas pipeline 104 to control the flow rate of the combustion gas.

[0108] In a more specific embodiment, a burner is provided at the air inlet end of the combustion gas pipeline 104 for igniting the combustion gas to provide heat for the pyrolysis reaction.

[0109] In a specific embodiment, the primary pyrolysis reactor 100, the secondary pyrolysis reactor 101 and the tertiary pyrolysis reactor 102 are respectively provided with a pressure sensor and / or a temperature sensor for real-time monitoring of the reaction temperature and reaction pressure in the primary pyrolysis reactor 100, the secondary pyrolysis reactor 101 and the tertiary pyrolysis reactor 102.

[0110] In a more specific embodiment, the pyrolysis component 10 also includes a pyrolysis process controller 107, which is connected to the pressure sensor and / or temperature sensor signal, and is used to control the combustion gas supply of the pyrolysis component 10 based on the obtained temperature signal, and determine whether to issue a safety warning based on the obtained pressure signal. The pyrolysis component 10 is also provided with an intelligent control unit, which is connected to the pressure sensor and / or the temperature sensor and / or the humidity sensor, and is used to receive data from the pressure sensor and / or the temperature sensor and / or the humidity sensor. The intelligent control unit is used to accurately control the temperature and humidity of the pyrolysis reactor, and monitor the pressure in the pyrolysis reactor to ensure safe production.

[0111] In a Figure 2 In the specific embodiment shown, the high-efficiency continuous oily sludge pyrolysis device also includes a pretreatment component 20; the pretreatment component 20 is arranged upstream of the pyrolysis component 10, and is used to pretreat the oily sludge to be pyrolyzed and then transport it to the pyrolysis component 10; the pretreatment component 20 includes a pretreatment unit, a conveying unit and an oily sludge pipeline 103 in sequence along the process direction.

[0112] In a Figure 2 In the more specific embodiment shown, the pretreatment unit includes a filter press 201 and a pulverizer 203 in sequence along the process direction. Specifically, the filter press 201 is a plate-frame filter press, and the water content of the oily sludge treated by the filter press 201 is 20-30wt%, and the particle size of the oily sludge treated by the pulverizer 203 is not more than 5mm. The oily sludge is preliminarily dehydrated by the filter press 201 to reduce the water content of the oily sludge entering the pyrolysis reactor and save energy consumption, and is further crushed by the pulverizer 203 to obtain small particles of oily sludge, thereby improving the pyrolysis efficiency and the recovery rate of pyrolysis oil.

[0113] In a Figure 2 In the further specific embodiment shown, the pretreatment unit further includes a slag storage tank 202, which is located downstream of the filter press 201. The slag storage tank 202 is used to store the material after the water removal treatment by the filter press 201, and transport the material to the crusher 203 for further crushing.

[0114] In a Figure 2 In the further specific embodiment shown, the feed end of the filter press 201 is connected to an oily sludge storage tank 208, a feed pump 209 and a feed flow meter 210. The feed flow meter 210 is used to detect the mass flow of the oily sludge entering the thermal treatment device.

[0115] In a Figure 2 In the more specific embodiment shown, the conveying unit includes a conveyor belt 204 , a bucket elevator 205 , a silo 206 and a screw feeder 207 in sequence along the process direction, and the screw feeder 207 is connected to the oily sludge pipeline 103 .

[0116] In a Figure 3 In the specific embodiment shown, the oily sludge pyrolysis device further includes a pyrolysis gas recovery component 30, which is connected to the pyrolysis gas exhaust end of the pyrolysis component 10 through a pipeline, and is used to post-treat the pyrolysis gas exhaust gas of the pyrolysis component 10 to obtain light oil and heavy oil respectively; along the process direction, the pyrolysis gas recovery component 30 includes a pyrolysis gas condenser 300, a centrifugal separator 301 and an oil phase fractionation tower 304 that are connected in sequence. The pyrolysis gas escaping from the primary pyrolysis reactor 100 is recycled. The pyrolysis gas is cooled, separated from oil and water, and fractionated to obtain light oil and heavy oil.

[0117] In a Figure 3 In the more specific embodiment shown, the centrifuge 301 is connected to the feed port of the oil phase fractionation tower 304 through an oil phase pipeline.

[0118] In a Figure 3 In the further specific embodiment shown, the oil phase pipeline is further provided with an oil storage tank 302 and / or an oil pump 303 and / or a flow meter 311. The flow meter 311 is used to detect the mass flow of the pyrolysis oil on the oil phase pipeline.

[0119] In a Figure 3 In the more specific embodiment shown, the light oil discharge end of the oil phase fractionation tower 304 is also connected to a fractionation condenser 305 and a gas-liquid separator 306 in sequence through pipelines. After the fractionation, the light component is cooled and the gas-liquid is separated to obtain light oil.

[0120] In a Figure 3 In the further specific embodiment shown, the gas-liquid separator 306 is connected to the tail gas absorption tower 307 through a gas pipeline. The gas components separated by the gas-liquid separator 306 include harmful gases such as hydrogen chloride, hydrogen sulfide and ammonia, which are absorbed and purified by the tail gas absorption tower 307 before being discharged.

[0121] In a Figure 3In the more specific embodiment shown, a fractionation reboiler 309 is further provided at the bottom of the oil phase fractionation tower 304, which is used to further fractionate the bottom oil phase of the oil phase fractionation tower 304 to obtain heavy oil and secondary light oil for reflux to the oil phase fractionation tower 304. The bottom oil phase remaining after fractionation and further fractionation is heavy oil.

[0122] In a Figure 3 In the more specific embodiment shown, the centrifuge 301 is also connected to a water phase pipeline and a water phase storage element 310 .

[0123] In a Figure 3 In the more specific embodiment shown, the centrifugal separator 301 is further connected to a tail gas absorption tower 307 through a gas phase pipeline. The gas components separated by the centrifugal separator 301 include harmful gases such as hydrogen chloride, hydrogen sulfide and ammonia, which are discharged after being absorbed and purified by the tail gas absorption tower 307. The tail gas absorption tower 307 can be an absorption tower for this type of tail gas commonly used in the prior art, for example, an alkaline solution absorption liquid or adsorbent can be used to absorb the tail gas.

[0124] In a Figure 3 In the further specific embodiment shown, an air pump 308 is provided on the gas phase pipeline.

[0125] This embodiment also provides a specific Figure 4 The high-efficiency continuous oily sludge pyrolysis device shown has the following process flow for pyrolysis reaction:

[0126] First, the oily sludge in the oily sludge storage tank 208 is pumped into the filter press 201 for filtration, and the obtained sludge is stored in the sludge storage tank 202, and then transferred to the pulverizer 203 for crushing treatment to obtain granular oily sludge with a particle size of no more than 5 mm and a water content of 20-30 wt%, and then transported to the silo 206 through the conveyor belt 204 and the bucket elevator 205, and flows into the feed port of the screw feeder 207 from the bottom outlet of the silo 206. Under the rotation of the screw feeder 207, the granular oily sludge moves to the discharge port of the screw feeder 207, and then enters the first pyrolysis reactor through the oily sludge pipeline 204. 100 for a primary pyrolysis reaction. After the primary pyrolysis reaction is completed, the first screw propeller transports the granular oily sludge to the first oily sludge discharge port, and enters the second pyrolysis reactor 101 through the oily sludge pipeline 103 for a secondary pyrolysis reaction. After the secondary pyrolysis reaction is completed, the second screw propeller transports the granular oily sludge to the second oily sludge discharge port, and enters the third pyrolysis reactor 103 through the oily sludge transport pipeline 104 for a tertiary pyrolysis reaction. After the tertiary pyrolysis reaction is completed, the third screw propeller transports the granular oily sludge to the third oily sludge discharge port, and outputs the carbon residue through the oily sludge pipeline 103. The pyrolysis gas generated in the third pyrolysis reactor enters the second pyrolysis reactor and the first pyrolysis reactor through the pyrolysis gas pipeline 106, and is mixed with the incompletely pyrolyzed oily sludge to further promote the decomposition and conversion of the oily sludge. After the pyrolysis gas is cooled by the pyrolysis gas condenser 300, it is separated and treated by the centrifugal separator 301. The separated gas components enter the tail gas absorption tower 307 along the gas phase pipeline for treatment and then discharged. The separated water enters the water phase storage component 310 along the water phase pipeline. The separated oil components are fractionated by the oil phase fractionation tower 304. The liquid components obtained by the fractionation enter the fractionation reboiler 309 for further fractionation, and the gas components obtained by further fractionation enter the oil phase fractionation tower 304. The residual liquid components in the oil phase fractionation tower 304 are recovered; the gas components obtained by the fractionation enter the gas-liquid separator 306 for separation after condensation treatment, and the separated gas components enter the tail gas absorption tower 307 through the gas pipeline for treatment and then discharged, and the separated liquid components are recovered.

[0127] Before the pyrolysis reaction, the combustion gas passes through the combustion gas pipeline 104, and after ignition, the combustion gas enters the second combustion chamber 1011 and the first combustion chamber 1001 in sequence through the combustion gas pipeline 104, and then enters the combustion gas tail gas treatment unit 105 through the pipeline for treatment and then is discharged. During the pyrolysis reaction, the temperature and pressure of the pyrolysis reactor are monitored in real time according to the temperature sensor and the pressure sensor, and the flow rate of the combustion gas and the protection warning are adjusted by feedback.

[0128] Example 2

[0129] Example 2 adopts the same method as in Example 1 Figure 4The high-efficiency continuous oily sludge pyrolysis device shown treats an oily sludge.

[0130] The oily sludge is refinery sludge (water content is 60wt%, oil content is 25wt%), and after being treated by the plate and frame filter press 201, the water content is 20wt%, and then it is crushed into granular oily sludge with a particle size not greater than 5mm.

[0131] The combustion gas includes natural gas and air in a volume ratio of 1:10.

[0132] The propeller is a huge roller, and the roller cavity is filled with inert gas.

[0133] The reaction temperature of the first pyrolysis reactor is 350°C, the pressure is 0.1MPa, and the pyrolysis time is 0.5h; the reaction temperature of the first pyrolysis reactor is 500°C, the pressure is 0.1MPa, and the pyrolysis time is 0.5h; the reaction temperature of the third pyrolysis reactor is 600°C, the pressure is 0.1MPa, and the pyrolysis time is 1h.

[0134] The recovery rate of pyrolysis oil is 70wt%, of which, based on the mass of pyrolysis oil, the content of light oil is 80wt%, the content of heavy oil is 10wt%, and the remainder is tail gas. The weight of oily sludge is reduced by 77.5wt%, and the oil content of carbon residue is 2.5‰, which meets the discharge or reuse requirement of carbon residue oil content below 3‰ in the industry standard.

[0135] The oil content of carbon slag is tested using an infrared oil meter.

[0136] The recovery rate of pyrolysis oil = mass flow rate of pyrolysis oil / (oil content in oily sludge*mass flow rate of oily sludge)*100%.

[0137] The mass flow rate of pyrolysis oil is obtained by flow meter 311 , and the mass flow rate of oily sludge is obtained by feed flow meter 210 .

[0138] The test method for the moisture content of oily sludge is: calcine the oily sludge at 800°C to obtain carbon slag, calculate the slag content, and calculate the moisture content according to the following formula: moisture content = 1-oil content-slag content. Among them, the oil content of oily sludge is tested by infrared oil measuring instrument method.

[0139] by Figure 1 For reference, the weight reduction percentage of oily sludge is: the weight percentage of the difference between the weight of the treated oily sludge and the weight of the remaining carbon residue, based on the weight of the treated oily sludge. The higher the percentage, the better the reduction effect, which means that less oily sludge is formed into carbon residue and more enters Figure 3 The apparatus and process shown form valuable oils.

[0140] Example 3

[0141] Example 3 adopts the same method as in Example 1 Figure 4 The high-efficiency continuous oily sludge pyrolysis device shown treats an oily sludge.

[0142] The oily sludge is refinery sludge (water content 60wt%, oil content 30wt%), which has a water content of 20wt% after being treated by the plate and frame filter press 201, and is then crushed into granular oily sludge with a particle size not greater than 5mm.

[0143] The combustion gas includes natural gas and air in a volume ratio of 1:10.

[0144] The propeller is a huge roller, and the roller cavity is filled with inert gas.

[0145] The reaction temperature of the first pyrolysis reactor is 450°C, the pressure is 0.1MPa, and the pyrolysis is 1h; the reaction temperature of the first pyrolysis reactor is 550°C, the pressure is 0.1MPa, and the pyrolysis is 1h; the reaction temperature of the third pyrolysis reactor is 700°C, the pressure is 0.1MPa, and the pyrolysis is 2h.

[0146] The recovery rate of pyrolysis oil is 90wt%, of which, based on the mass of pyrolysis oil, the content of light oil is 85wt%, the content of heavy oil is 13wt%, and the remainder is tail gas. The weight of oily sludge is reduced by 87wt%, and the oil content of carbon residue is 1‰, which meets the discharge or reuse requirement of carbon residue oil content below 3‰ in the industry standard.

[0147] Comparative Example

[0148] This comparative example is a comparative example of Example 3, and is different from Example 3 in that the second pyrolysis reactor is not used, and the first pyrolysis reactor and the third pyrolysis reactor are directly connected with each other.

[0149] The oily sludge is refinery sludge (water content 60wt%, oil content 30wt%), which has a water content of 20wt% after being treated by the plate and frame filter press 201, and is then crushed into granular oily sludge with a particle size not greater than 5mm.

[0150] The reaction temperature of the first pyrolysis reactor is 450°C, the pressure is 0.1MPa, and the pyrolysis is carried out for 2h; the reaction temperature of the third pyrolysis reactor is 700°C, the pressure is 0.1MPa, and the pyrolysis is carried out for 2h.

[0151] The recovery rate of pyrolysis oil is 60wt%, of which, based on the mass of pyrolysis oil, the content of light oil is 60wt%, the content of heavy oil is 10wt%, and the remainder is tail gas. The weight of oily sludge is reduced by 79.5wt%, and the oil content of carbon residue is 7‰.

[0152] Compared with Example 3, the recovery rate of pyrolysis in this comparative example is relatively low, down by 30%; and the oil content of carbon residue is relatively high, exceeding the discharge or reuse requirement of carbon residue oil content below 3‰ in the industry standard.

[0153] The above embodiments are merely illustrative of the principles and effects of the present invention, and are not intended to limit the present invention. Anyone familiar with the art may modify or alter the above embodiments without departing from the spirit and scope of the present invention. Therefore, all equivalent modifications or alterations made by a person of ordinary skill in the art without departing from the spirit and technical concept disclosed by the present invention shall still be covered by the claims of the present invention.

Claims

1. A high-efficiency continuous oily sludge pyrolysis device, characterized in that: The invention comprises a pyrolysis component (10), wherein the pyrolysis component (10) comprises a primary pyrolysis reactor (100), a secondary pyrolysis reactor (101) and a tertiary pyrolysis reactor (102) which are connected to each other in sequence from top to bottom.

2. The high-efficiency continuous oily sludge pyrolysis device according to claim 1 is characterized in that: The primary pyrolysis reactor (100) comprises a first horizontal screw propeller for conveying materials, the secondary pyrolysis reactor (101) comprises a second horizontal screw propeller for conveying materials, and the tertiary pyrolysis reactor (102) comprises a third horizontal screw propeller for conveying materials; And / or, the primary pyrolysis reactor (100) comprises a first fuel gas chamber (1001) for providing reaction heat supply, the secondary pyrolysis reactor (101) comprises a second fuel gas chamber (1011) for providing reaction heat supply, and the tertiary pyrolysis reactor (102) comprises a third fuel gas chamber (1021) for providing reaction heat supply; And / or, the pyrolysis component (10) comprises an oily sludge pipeline (103), a combustion gas pipeline (104) and a pyrolysis gas pipeline (106); the oily sludge pipeline (103), the combustion gas pipeline (104) and the pyrolysis gas pipeline (106) are respectively connected to the primary pyrolysis reactor (100), the secondary pyrolysis reactor (101) and the tertiary pyrolysis reactor (102) in sequence, and the oily sludge pipeline (103) is used to allow the oily sludge to react step by step from top to bottom; the combustion gas pipeline (104) is used to allow the combustion gas to be supplied step by step from bottom to top; and the pyrolysis gas pipeline (106) is used to allow the pyrolysis gas to be transported step by step from bottom to top to participate in the pyrolysis reaction; And / or, the first-stage pyrolysis reactor (100), the second-stage pyrolysis reactor (101) and the third-stage pyrolysis reactor (102) are each provided with a pressure sensor and / or a temperature sensor and / or a humidity sensor.

3. The high-efficiency continuous oily sludge pyrolysis device according to claim 2 is characterized in that: The input ends of the oily sludge pipelines (103) corresponding to the primary pyrolysis reactor (100), the secondary pyrolysis reactor (101) and the tertiary pyrolysis reactor (102) and the gas inlet ends of the corresponding pyrolysis gas pipelines (106) are arranged at the same end of the corresponding pyrolysis reactors, so that the oily sludge and the pyrolysis gas are transported along the same material transport direction in the same-stage pyrolysis reactor; and / or, the combustion gas pipeline (104) is connected in sequence to the first combustion gas chamber (1001), the second combustion gas chamber (1011) and the third combustion gas chamber (1021); And / or, the pyrolysis component (10) further comprises a pyrolysis process controller (107), which is connected to the pressure sensor and / or the temperature sensor and / or the humidity sensor signal, and is used to control the combustion gas supply of the pyrolysis component (10) based on the obtained temperature signal, and to determine whether to issue a safety warning based on the obtained pressure signal; And / or, the pyrolysis assembly (10) further comprises a combustion gas tail gas processing unit (105), and the combustion gas tail gas processing unit (105) is connected to the combustion gas exhaust end of the primary pyrolysis reactor (100) through a pipeline; And / or, a flow control regulating valve is provided on the combustion gas pipeline (104); and / or, a gap d between the first horizontal screw propeller and the inner wall of the reaction chamber of the primary pyrolysis reactor (100) is 20 to 25 mm; and / or a gap d between the second horizontal screw propeller and the inner wall of the reaction chamber of the secondary pyrolysis reactor (101) is 20 to 25 mm; And / or, a gap d between the third horizontal screw propeller and the inner wall of the reaction chamber of the third-stage pyrolysis reactor (102) is 20 to 25 mm.

4. The high-efficiency continuous oily sludge pyrolysis device according to claim 1 is characterized in that: The high-efficiency continuous oily sludge pyrolysis device further comprises a pretreatment component (20); the pretreatment component (20) is arranged upstream of the pyrolysis component (10) and is used to pre-treat the oily sludge to be pyrolyzed and then transport it to the pyrolysis component (10); The pretreatment component (20) comprises a pretreatment unit, a conveying unit and the oily sludge pipeline (103) in sequence along the process direction; And / or, the oily sludge pyrolysis device further comprises a pyrolysis gas recovery component (30), wherein the pyrolysis gas recovery component (30) The pyrolysis gas recovery component (30) is connected to the pyrolysis gas exhaust end of the pyrolysis component (10) through a pipeline, and is used to post-treat the pyrolysis gas exhaust gas of the pyrolysis component (10) to obtain light oil and heavy oil respectively; along the process direction, the pyrolysis gas recovery component (30) includes a pyrolysis gas condenser (300), a centrifugal separator (301) and an oil phase fractionation tower (304) which are connected in sequence.

5. The high-efficiency continuous oily sludge pyrolysis device according to claim 4 is characterized in that: The centrifugal separator (301) is connected to the feed port of the oil phase fractionation tower (304) through an oil phase pipeline; more preferably, an oil storage tank (302) and / or an oil pump (303) and / or a flow meter (311) are further provided on the oil phase pipeline; And / or, the light oil discharge end of the oil phase fractionation tower (304) is also connected to a fractionation condenser (305) and a gas-liquid separator (306) in sequence through pipelines; preferably, the gas-liquid separator (306) is connected to the tail gas absorption tower (307) through a gas pipeline; And / or, a fractionation reboiler (309) is further provided at the bottom of the oil phase fractionation tower (304) for further fractionating the oil phase at the bottom of the oil phase fractionation tower (304) to obtain heavy oil and secondary light oil for reflux to the oil phase fractionation tower (304); And / or, the centrifugal separator (301) is further connected to a water phase pipeline and a water phase storage element (310); And / or, the centrifuge (301) is also connected to a tail gas absorption tower (307) via a gas phase pipeline.

6. The high-efficiency continuous oily sludge pyrolysis device according to claim 4 is characterized in that: The pretreatment unit includes a filter press (201) and a pulverizer (203) in sequence along the process direction; preferably, the feed end of the filter press (201) is connected to an oily sludge storage tank 208, a feed pump (209) and a feed flow meter (210); And / or, the conveying unit includes a conveyor belt (204), a bucket elevator (205), a silo (206) and a screw feeder (207) in sequence along the process direction, and the screw feeder (207) is connected to the oily sludge pipeline (103).

7. A method for continuously pyrolyzing oily sludge using the high-efficiency continuous oily sludge pyrolysis device as described in any one of claims 1 to 6.

8. The method according to claim 1, characterized in that Includes one or more of the following features: The reaction temperature of the primary pyrolysis reactor (100) is 350-450°C; The reaction pressure of the primary pyrolysis reactor (100) is 0.05-0.15 MPa; The heating rate of the primary pyrolysis reactor (100) is 5 to 20°C / min; The relative humidity of the primary pyrolysis reactor (100) during the reaction is 50-80% RH; The reaction time of the primary pyrolysis reactor (100) is 0.5 to 1 h; The reaction temperature of the secondary pyrolysis reactor (101) is 450-550°C; The reaction pressure of the secondary pyrolysis reactor (101) is 0.05-0.15 MPa; The heating rate of the secondary pyrolysis reactor (101) is 5 to 20°C / min; The relative humidity of the secondary pyrolysis reactor (101) during the reaction is 50-80% RH; The reaction time of the secondary pyrolysis reactor (101) is 0.5 to 1 hour; The reaction temperature of the three-stage pyrolysis reactor (102) is 550-700°C; The reaction pressure of the three-stage pyrolysis reactor (102) is 0.05-0.15 MPa; The heating rate of the three-stage pyrolysis reactor (102) is 5 to 20°C / min; The relative humidity of the three-stage pyrolysis reactor (102) during the reaction is 50-80% RH; The reaction time of the three-stage pyrolysis reactor (102) is 1 to 2 hours; The oily sludge is subjected to a primary pyrolysis reaction in the primary pyrolysis reactor (100), and the sludge outlet stream of the primary pyrolysis reactor (100) after the primary pyrolysis reaction enters the secondary pyrolysis reactor (101) for a secondary pyrolysis reaction, and the sludge outlet stream of the secondary pyrolysis reactor (101) after the secondary pyrolysis reaction enters the tertiary pyrolysis reactor (102) for a tertiary pyrolysis reaction; The pyrolysis component (10) is also provided with an intelligent control unit, which is connected to the pressure sensor and / or the temperature sensor and / or the humidity sensor and is used to receive data from the pressure sensor and / or the temperature sensor and / or the humidity sensor.

9. The method according to claim 8, characterized in that Includes one or more of the following features: The combustion gas includes natural gas and air, with a volume ratio of 1:(10-15); The combustion gas enters the second gas chamber (1011) and the first gas chamber (1001) in sequence from the third gas chamber (1021); The pyrolysis gas enters the secondary pyrolysis reactor (101) and the primary pyrolysis reactor (100) in sequence from the tertiary pyrolysis reactor (102); The water content of the oily sludge treated by the filter press (201) is 20 to 30 wt%; The particle size of the oily sludge treated by the pulverizer (203) is no greater than 5 mm; The combustion gas escaping from the first combustion chamber (1001) is discharged after being treated; Recycling the pyrolysis gas emitted from the primary pyrolysis reactor (100); The intelligent control unit is connected to the flow control regulating valve signal and is used to adjust the flow size of the flow control regulating valve according to the control instruction; The intelligent control unit comprises an alarm module, and the intelligent control unit is connected to the alarm module signal to trigger a safety warning according to a control instruction.

10. The method according to claim 9, characterized in that The pyrolysis gas is cooled, separated from oil and water, and fractionated to obtain light oil and heavy oil; preferably, the light component after distillation is cooled and separated from gas and liquid to obtain light oil; preferably, the bottom oil phase remaining after distillation and further distillation is heavy oil.

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