CN112707615A

CN112707615A - Device and method for liquid-containing oil sludge co-processing by condensation of pyrolysis gas

Info

Publication number: CN112707615A
Application number: CN202011621030.6A
Authority: CN
Inventors: 金兆迪; 张哲娜; 丛培超; 孙启刚; 谢金坤; 牛玉国
Original assignee: Jereh Environmental Protection Technology Co Ltd
Current assignee: Jereh Environmental Protection Technology Co Ltd
Priority date: 2020-12-31
Filing date: 2020-12-31
Publication date: 2021-04-27
Also published as: WO2022141677A1

Abstract

The embodiment of the disclosure provides a device and a method for the pyrolysis gas condensation cooperative treatment of liquid-containing oil sludge, and the method for the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge comprises the following steps: providing liquid-containing oil sludge and pyrolysis gas; and (2) contacting the liquid-containing oil sludge with the pyrolysis gas to carry out heat exchange so as to condense at least part of an oil phase in the pyrolysis gas, and evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge to obtain oil-water vapor and a solid-containing oil phase.

Description

Device and method for liquid-containing oil sludge co-processing by condensation of pyrolysis gas

Technical Field

The embodiment of the disclosure relates to a device and a method for the cooperative treatment of liquid-containing oil sludge by pyrolysis gas condensation.

Background

The thermal desorption technology is that a heat source is utilized to heat the oily waste, organic matters and water in the oily waste are evaporated and pyrolyzed to form pyrolysis gas under the anaerobic condition, so that the organic matters and the water are separated from a solid phase, and petroleum resources in the pyrolysis gas are recovered through condensation, thereby realizing the harmless treatment and resource utilization of the oily waste.

Oily sludge is one of the main pollutants generated in the processes of oil and gas field development, refining, gathering, transportation and storage. The oily sludge has complex components, mainly consists of water, clay particles, various oils, asphaltene, bacterial substances, toxic and harmful non-degradable organic substances and the like, has serious harm to water sources and soil, and can affect the ecological environment and the health of human beings. Therefore, the oily sludge must be treated.

Disclosure of Invention

At least one embodiment of the present disclosure provides a method for cooperatively treating liquid-containing oil sludge by pyrolysis gas condensation, including: providing liquid-containing oil sludge and pyrolysis gas; and contacting the liquid-containing oil sludge with the pyrolysis gas for heat exchange so as to condense at least part of an oil phase in the pyrolysis gas, and evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge to obtain oil-water vapor and a solid-containing oil phase.

For example, in a method for the cooperative processing of liquid-containing oil sludge by pyrolysis gas condensation provided by at least one embodiment of the present disclosure, a shielding gas is mixed into the liquid-containing oil sludge before the liquid-containing oil sludge is contacted with the pyrolysis gas.

For example, in the method for the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge provided by at least one embodiment of the present disclosure, the flow rate of the liquid-containing oil sludge is adjusted so that the temperature of the obtained oil-water vapor is in the range of 100 ℃ to 200 ℃.

For example, in at least one embodiment of the present disclosure, the method for treating liquid-containing oil sludge by using pyrolysis gas condensation and cooperation, the contacting the liquid-containing oil sludge and the pyrolysis gas for heat exchange includes: and conveying the liquid-containing oil sludge to a liquid inlet of a tank body, conveying the pyrolysis gas to a gas inlet of the tank body, and contacting the liquid-containing oil sludge and the pyrolysis gas in the tank body to perform heat exchange.

For example, in the method for the condensation and cooperative treatment of liquid-containing oil sludge by pyrolysis gas provided by at least one embodiment of the present disclosure, a sprayer is disposed in the tank, the sprayer is communicated with the liquid inlet, and the liquid-containing oil sludge is sprayed to the pyrolysis gas through the sprayer, so that the liquid-containing oil sludge is in contact with the pyrolysis gas for heat exchange.

For example, in a method of co-processing liquid-containing sludge by pyrolysis gas condensation provided by at least one embodiment of the present disclosure, during the transportation of the liquid-containing sludge to the liquid inlet, at least one of a booster pump and a liquid phase regulating valve is used to regulate the flow rate of the liquid-containing sludge.

For example, in a method for the pyrolysis gas condensation cooperative treatment of liquid-containing oil sludge provided in at least one embodiment of the present disclosure, the tank further includes an exhaust port for exhausting the oil-water vapor, and a temperature transmitter is disposed in a transfer passage for exhausting the oil-water vapor from the exhaust port, and the method further includes: and the temperature of the oil vapor is controlled to be between 100 and 200 ℃ through the interlocking control of the temperature transmitter and the liquid phase regulating valve.

For example, at least one embodiment of the present disclosure provides a method for the pyrolysis gas condensation synergistic treatment of liquid-containing oil sludge, further including: condensing the oil-water vapor to obtain an oil-water mixture and a non-condensable gas; carrying out oil-water separation on the oil-water mixture to obtain light oil and oily wastewater; and collecting the non-condensable gas.

For example, at least one embodiment of the present disclosure provides a method for the pyrolysis gas condensation synergistic treatment of liquid-containing oil sludge, further including: and settling and separating the solid oil-containing phase to obtain heavy oil and an oil-containing solid phase.

At least one embodiment of the present disclosure further provides a device for the pyrolysis gas condensation cooperative treatment of liquid-containing oil sludge, including: the first tank comprises a first liquid inlet and a first air inlet; a first conduit in communication with a source of liquid-containing sludge and extending to the first inlet; a second pipeline communicated with a pyrolysis gas source and extending to the first gas inlet; wherein the first conduit is configured to convey liquid-containing sludge derived from the source of liquid-containing sludge to the first inlet port, the second conduit is configured to convey pyrolysis gas derived from the source of pyrolysis gas to the first inlet port, and the liquid-containing sludge and the pyrolysis gas are contacted in the first tank for heat exchange.

For example, at least one embodiment of the present disclosure provides an apparatus for cooperatively treating liquid-containing oil sludge by pyrolysis gas condensation, further including: the liquid phase regulating valve is arranged between the booster pump and the first liquid inlet.

For example, the apparatus for the condensation and cooperative treatment of liquid-containing oil sludge by using pyrolysis gas further includes a sprayer disposed in the first tank, where the sprayer is communicated with the first liquid inlet, the first liquid inlet and the sprayer are disposed at an upper portion of the first tank, and the first gas inlet is disposed at a lower portion of the first tank.

For example, in an apparatus for the co-treatment of liquid-containing oil sludge by condensation of pyrolysis gas provided by at least one embodiment of the present disclosure, the spray header includes a plurality of spray headers, and the plurality of spray headers are arranged in one or more rows.

For example, the apparatus for the cooperative processing of liquid-containing oil sludge by pyrolysis gas condensation provided by at least one embodiment of the present disclosure further includes a third pipeline communicated with the shielding gas source, wherein the first tank further includes a second gas inlet at a top thereof, and the third pipeline extends to the second gas inlet.

For example, in the apparatus for co-processing liquid-containing oil sludge by pyrolysis gas condensation provided by at least one embodiment of the present disclosure, the second gas inlet is communicated between the sprayer and the first liquid inlet, so that the protective gas and the liquid-containing oil sludge are mixed and then are conveyed to the sprayer.

For example, at least one embodiment of the present disclosure provides an apparatus for the cooperative treatment of liquid-containing oil sludge by condensation of pyrolysis gas, further comprising a condenser, wherein the first tank comprises a first exhaust port disposed at a top portion thereof, the condenser comprises a second tank comprising a third intake port, and the first exhaust port is connected to the third intake port.

For example, in the apparatus for co-processing liquid-containing oil sludge by condensing pyrolysis gas provided in at least one embodiment of the present disclosure, a temperature transmitter is disposed on a pipeline connecting the first exhaust port and the third intake port, and the liquid phase regulating valve and the temperature transmitter are controlled in an interlocking manner to control the temperature of oil-water vapor discharged from the first exhaust port to be 100 ℃ to 200 ℃.

For example, in the apparatus for the condensation synergistic treatment of liquid-containing oil sludge by using pyrolysis gas provided by at least one embodiment of the present disclosure, the condenser further includes an oil-water separator, the second tank includes a first liquid discharge port disposed at the bottom thereof, the oil-water separator includes a second liquid inlet disposed at the top thereof, and the first liquid discharge port is communicated with the second liquid inlet.

For example, the apparatus for the cooperative processing of liquid-containing oil sludge by pyrolysis gas condensation provided by at least one embodiment of the present disclosure further includes an oil separator, where the first tank further includes a second liquid outlet disposed at a bottom thereof, and the oil separator includes a third liquid inlet, and the second liquid outlet is communicated with the third liquid inlet.

Drawings

In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings of the embodiments will be briefly described below, and it is apparent that the drawings in the following description only relate to some embodiments of the present invention and are not limiting on the present invention.

Fig. 1 is a block diagram illustrating a structure of an apparatus for co-processing liquid-containing oil sludge by condensing pyrolysis gas according to an embodiment of the disclosure;

fig. 2 is a block diagram illustrating a structure of an apparatus for co-processing liquid-containing oil sludge by pyrolysis gas condensation according to still another embodiment of the disclosure;

fig. 3 is a flow chart of pyrolysis gas condensation cooperative treatment of liquid-containing oil sludge according to an embodiment of the disclosure;

FIG. 4 is a flow chart of the pyrolysis gas condensation co-processing of liquid-containing sludge according to yet another embodiment of the disclosure;

FIG. 5 is a flow chart of the pyrolysis gas condensation co-processing of liquid-containing sludge according to yet another embodiment of the disclosure;

FIG. 6 is a flow chart of the pyrolysis gas condensation co-processing of liquid-containing sludge according to yet another embodiment of the disclosure;

FIG. 7 is a flow chart of the pyrolysis gas condensation co-processing of liquid-containing sludge according to yet another embodiment of the disclosure;

FIG. 8 is a flow chart of the pyrolysis gas condensation co-processing of liquid-containing sludge according to yet another embodiment of the disclosure;

FIG. 9 is a flow chart of the pyrolysis gas condensation co-processing of liquid-containing sludge according to yet another embodiment of the disclosure; and

fig. 10 is a flow chart of the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge according to still another embodiment of the disclosure.

Detailed Description

In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the drawings of the embodiments of the present invention. It is to be understood that the embodiments described are only a few embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the described embodiments of the invention without any inventive step, are within the scope of protection of the invention.

Unless defined otherwise, technical or scientific terms used herein shall have the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs. The use of "first," "second," and similar terms in this disclosure is not intended to indicate any order, quantity, or importance, but rather is used to distinguish one element from another. The word "comprising" or "comprises", and the like, means that the element or item listed before the word covers the element or item listed after the word and its equivalents, but does not exclude other elements or items. The terms "connected" or "coupled" and the like are not restricted to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "upper", "lower", "top", "bottom", and the like are used merely to indicate relative positional relationships, and when the absolute position of the object being described is changed, the relative positional relationships may also be changed accordingly.

At present, high-temperature pyrolysis gas generated by thermal desorption is mostly condensed by adopting a direct spraying or indirect cooling mode. When the indirect cooling mode is adopted, the cooling medium is mostly circulating water or circulating oil in the system, but the heat released by the condensation of the high-temperature pyrolysis gas cannot be effectively utilized, so that the resource waste is caused. For example, when the mode of direct spraying is adopted, the high-temperature pyrolysis gas is condensed by adopting the sedimentation separation water, and meanwhile, the high-temperature pyrolysis gas also heats the circulating sedimentation separation water, so that the sedimentation separation water is further recycled, heat exchange equipment and external cooling water are needed to cool the sedimentation separation water, and therefore additional energy consumption is increased. Therefore, the optimization of the high-temperature pyrolysis gas condensation process is needed to realize the utilization of the waste heat of the high-temperature pyrolysis gas.

At present, a plurality of technologies for treating the liquid-containing oil sludge exist, but different problems exist, and for the liquid-containing oil sludge with high liquid content rate, such as oil-containing wastewater scum, aging oil, oil-containing emulsion and the like, the energy consumption of directly adopting a thermal desorption technology is high, and the economical efficiency is poor; by adopting the incineration mode, the heat utilization rate is low, the requirement on the heat value of the raw material is met, the petroleum resource cannot be recovered, and dust pollution and gas pollution can be generated; because the oily wastewater scum, aging oil, oily emulsion and the like have strong stability, the dehydration process is difficult by adopting conventional methods such as concentration, dehydration, chemical demulsification and the like, the effective separation of oil and water is difficult to realize even if conventional medicaments are added, and the quality of the oil recovered after the treatment of the medicaments is poor.

The inventor of the present disclosure has noticed that the temperature of the high-temperature pyrolysis gas can reach 250-550 ℃, if circulating water, circulating oil or settling separation water and the like are specially adopted to condense the high-temperature pyrolysis gas, the heat of the high-temperature pyrolysis gas cannot be utilized, and the consumption of the circulating water, the circulating oil and the settling separation water is very large, thereby causing a great deal of resource waste. The inventor of this disclosure also noted simultaneously that heating the oily sludge containing liquid that contains the liquid rate height is favorable to retrieving the oil resource wherein, consequently, can adopt high temperature pyrolysis gas to heat oily sludge containing liquid, adopts oily sludge containing liquid to condense high temperature pyrolysis gas simultaneously, has just so realized pyrolysis gas condensation coprocessing oily sludge containing liquid to make the resource obtain the maximize utilization, and avoided wasting of resources and environmental pollution. For example, the high-temperature pyrolysis gas is contacted with the liquid-containing oil sludge for heat exchange so as to condense the high-temperature pyrolysis gas, so that at least part of the oil phase in the high-temperature pyrolysis gas is condensed; the liquid-containing oil sludge is heated, so that the water phase and at least part of the oil phase in the liquid-containing oil sludge are evaporated, more oil resources can be recovered without increasing extra energy consumption, the separation of the oil and the water in the liquid-containing oil sludge is realized without using any chemical agent, and the oil resources in the liquid-containing oil sludge are recovered to obtain high-quality oil resources.

At least one embodiment of the present disclosure provides an apparatus for cooperatively processing liquid-containing oil sludge by condensing pyrolysis gas, for example, fig. 1 is a block diagram illustrating a structure of an apparatus for cooperatively processing liquid-containing oil sludge by condensing pyrolysis gas according to an embodiment of the present disclosure, and as shown in fig. 1, the apparatus 1 for cooperatively processing liquid-containing oil sludge by condensing pyrolysis gas includes: a first tank 10, a first pipeline 13 and a second pipeline 14, wherein the first tank 10 comprises a first liquid inlet 11 and a first gas inlet 12. The first conduit 13 is in communication with a source of liquid-containing sludge and extends to the first inlet port 11, the second conduit 14 is in communication with a source of pyrolysis gas and extends to the first inlet port 12, the first conduit 13 is arranged to convey liquid-containing sludge derived from the source of liquid-containing sludge to the first inlet port 11, the second conduit 14 is arranged to convey pyrolysis gas derived from the source of pyrolysis gas to the first inlet port 12, and the liquid-containing sludge and the pyrolysis gas are contacted in the first tank 10 for heat exchange.

For example, the first line 13 extending to the first loading port 11 means that the first line 13 is in communication with the first loading port 11 and the first line 13 may convey liquid-containing sludge to the first loading port 11. The extension of the second pipeline 14 to the first gas inlet 12 means that the second pipeline 14 is connected to the first gas inlet 12, and the second pipeline 14 can transmit the pyrolysis gas to the first gas inlet 12.

For example, the liquid-containing oil sludge is a fluid oil sludge, and the total mass percentage of water and oil in the liquid-containing oil sludge is 70% to 95%. For example, the mass percentages of water and oil in the liquid-containing sludge are 70%, 75%, 80%, 85%, 90% or 95%, which can ensure that the liquid-containing sludge flows well in the first pipeline 13 and that the liquid-containing sludge condenses the pyrolysis gas well.

For example, pyrolysis gas is generated by subjecting oil-containing waste to thermal desorption treatment. The thermal desorption process is that organic pollutants in the oily waste are subjected to evaporation, pyrolysis and other actions under the high-temperature anaerobic condition, finally, oil and water in the oily waste are thoroughly separated from a solid phase, and petroleum resources are recycled, so that harmless treatment and resource utilization of the oily waste are realized. For example, the thermal desorption treatment can be carried out in one or more pyrolysis furnaces, the temperature of the thermal desorption treatment is controlled to be 250-550 ℃, the time of the thermal desorption is controlled to be 0.4-3.2 h, and the temperature of the finally formed pyrolysis gas is 250-550 ℃. For example, the temperature of the pyrolysis gas is 250 ℃, 300 ℃, 350 ℃, 400 ℃, 450 ℃, 500 ℃ or 550 ℃.

For example, the heavy oil component in the pyrolysis gas condenses into a liquid phase, the stability of the liquid-containing sludge is destroyed by the heating action of the pyrolysis gas, the emulsifiability is reduced, and the water component and the light oil component in the liquid-containing sludge are heated by the pyrolysis gas to form water vapor and oil vapor. After cooling by the liquid-containing sludge, the uncondensed gas phase in the pyrolysis gas is mixed with the oil vapor and the water vapor evaporated from the liquid-containing sludge to form oil vapor.

For example, the first inlet port 11 is closer to the top of the first tank 10 than the first inlet port 12.

It should be noted that, when the apparatus for processing liquid-containing oil sludge by using pyrolysis gas condensation and cooperation works normally, liquid flows in a first direction under the action of gravity, the surface of the first tank 10 on the opposite side of the first direction is the top of the first tank 10, and the surface of the first tank 10 on the same side of the first direction is the bottom of the first tank 10.

For example, as the liquid-containing sludge is subjected to gravity, it will flow downwardly (i.e. in a direction away from the top of the first tank 10 within the first tank 10) after flowing into the first tank 10 from the first inlet 11; due to the large intermolecular spacing, and particularly the low density, of the pyrolysis gas, the pyrolysis gas will flow upward (i.e., in the direction of the top of the first tank 10 within the first tank 10) after entering the first tank 10 from the first gas inlet 12. In this way, the liquid-containing sludge fed from the first liquid inlet 11 closer to the top of the first tank 10 flows downwards under the action of gravity, and the surface contacting with the upwardly flowing pyrolysis gas fed from the first gas inlet 12 is more, so that the liquid-containing sludge and the pyrolysis gas are contacted more fully, and the heat exchange process is more complete.

It should be noted that the distance from the first air inlet 12 to the top of the first tank 10 and the distance from the first liquid inlet 11 to the top of the first tank 10 may be approximately equal; alternatively, the first liquid inlet 11 may be further away from the top of the first tank 10 than the first gas inlet 12, which is not limited by the embodiment of the disclosure.

For example, as shown in fig. 1, the apparatus 1 for co-processing liquid-containing sludge by pyrolysis gas condensation further comprises a booster pump 15 disposed on the first pipeline 13, and a liquid phase regulating valve 16 disposed between the booster pump 15 and the first liquid inlet 11. The booster pump 15 and the liquid phase regulating valve 16 can both regulate the flow rate of the liquid-containing sludge.

For example, the booster pump 15 may regulate the flow rate of the liquid-containing sludge by increasing the transport rate of the liquid-containing sludge, i.e. providing power to the flow of the liquid-containing sludge. The liquid phase regulating valve 16 may adjust the input of the liquid-containing sludge to regulate the flow rate of the liquid-containing sludge, thereby ensuring that a sufficient amount of the liquid-containing sludge is in sufficient contact with the pyrolysis gas. The liquid phase regulating valve 16 can also control the temperature of the oil vapor in interlock with a temperature transmitter mentioned later.

For example, the opening degree of the valve of the liquid phase control valve 16 is automatically controlled based on a signal from the control portion, thereby controlling the flow rate of the liquid-containing sludge.

The liquid phase regulating valve 16 includes, for example, an electric regulating valve, a pneumatic regulating valve, a hydraulic regulating valve, and the like.

For example, as shown in fig. 1, the apparatus for the pyrolysis gas condensation cooperative treatment of liquid-containing oil sludge according to at least one embodiment of the present disclosure further includes a sprayer 17 disposed in the first tank 10, the sprayer 17 is communicated with the first liquid inlet 11, the first liquid inlet 11 and the sprayer 17 are disposed at an upper portion of the first tank 10, and the first gas inlet 12 is disposed at a lower portion of the first tank 10. The liquid-containing oil sludge enters from the first liquid inlet 11 and is conveyed to a sprayer 17 communicated with the first liquid inlet 11, the sprayer 17 is configured to spray the liquid-containing oil sludge to the pyrolysis gas input through the first gas inlet 12, and the pyrolysis gas is condensed through the spraying of the sprayer 17, so that the liquid-containing oil sludge and the pyrolysis gas are in more sufficient contact.

For example, by providing the first liquid inlet 11 and the shower 17 at the upper portion of the first tank 10 and providing the first gas inlet 12 at the lower portion of the first tank 10, both the liquid-containing sludge sprayed from the shower 17 can be brought into contact with the pyrolysis gas entering from the first gas inlet 12, the pyrolysis gas can be sufficiently sprayed and cooled, and the formed oil-water vapor can be quickly discharged while rising.

For example, as shown in fig. 1, the first can 10 is divided into a first portion 101 and a second portion 102 along a horizontal center line a-a', an upper portion of the first can 10 is the first portion 101 closer to the top of the first can 10, and a lower portion of the first can 10 is the second portion 102 farther from the top of the first can 10.

For example, the shower 17 includes a plurality of shower heads 171, and the plurality of shower heads 171 are disposed in one or more rows. In the configuration shown in fig. 1, 3 showerheads 171 are arranged in a row. For example, it is also possible that the plurality of shower heads 171 are arranged in one or more rows so that the area between the first side wall and the second side wall of the first tank 10 can spray the sludge containing liquid.

The plurality of shower heads 171 are arranged in a plurality of rows, and the plurality of rows may be formed by arranging the plurality of shower heads 171 in a plurality of rows on a plane at the same height, or may be formed by arranging the plurality of shower heads 171 in a plurality of rows on planes at different heights. The plurality of showerheads 171 may be disposed along the circumference of the inner edge of the first can body 10, or may be disposed only in the center of the first can body 10, which is not limited in the embodiments of the present disclosure.

For example, the shower head 171 includes a multi-head atomizing nozzle, a square nozzle, a high-pressure cleaning nozzle, a hollow cone nozzle, a fan nozzle, a spiral nozzle, and the like.

For example, in some embodiments, it is also possible that the sprayer 17 comprises a spray header 171, which is a multi-head atomizing nozzle or a fan nozzle, so as to ensure that the liquid-containing sludge sprayed from the spray header 171 covers a sufficiently large area, so that the liquid-containing sludge and the pyrolysis gas are in more sufficient contact, and thus the heat exchange process between the liquid-containing sludge and the pyrolysis gas is more sufficient.

For example, as shown in fig. 1, the apparatus for the condensation and co-processing of the pyrolysis gas and the liquid-containing oil sludge provided by at least one embodiment of the present disclosure further includes a third pipeline 18 communicated with the shielding gas source, the first tank 10 further includes a second gas inlet 19 at the top thereof, the third pipeline 18 extends to the second gas inlet 19, the third pipeline 18 is configured to deliver the shielding gas obtained from the shielding gas source to the second gas inlet 19, and the shielding gas can prevent the gas volatilized from the liquid-containing oil sludge or the pyrolysis gas from being oxidized by the oxygen remaining in the first tank 10 or the oxygen brought in the process of delivering the liquid-containing oil sludge under high temperature conditions.

For example, the third pipeline 18 extending to the second gas inlet 19 means that the third pipeline 18 is communicated with the second gas inlet 19, and the third pipeline 18 can transmit the shielding gas to the second gas inlet 19.

For example, the second gas inlet 19 is located at the top of the first tank 10, which facilitates the communication between the second gas inlet 19 and the first liquid inlet 11 and the sprayer 17, thereby reducing the length of the pipeline located in the first tank 10, and simultaneously facilitating the downward flow of the shielding gas for directly mixing with the liquid-containing sludge.

For example, the second gas inlet 19 is connected between the shower 17 and the first liquid inlet 11, so that the protective gas entering from the second gas inlet 19 is conveyed between the shower 17 and the first liquid inlet 11, so that the liquid-containing sludge entering from the first liquid inlet 11 is mixed with the protective gas, and then the mixture of the protective gas and the liquid-containing sludge is conveyed to the shower 17.

For example, the protective gas and the liquid-containing sludge are mixed and then conveyed to the sprayer 17, so that the contact area of the liquid-containing sludge and the pyrolysis gas is larger when spraying, and the heat exchange between the liquid-containing sludge and the pyrolysis gas is more sufficient.

For example, the apparatus for co-processing liquid-containing sludge by pyrolysis gas condensation further comprises a gas regulating valve 20 disposed on the third pipeline 18, wherein the gas regulating valve 20 is configured to regulate the flow of the shielding gas. For example, the opening of the valve of the gas regulating valve 20 can be automatically controlled according to the signal of the regulating part, thereby realizing the regulation of the flow rate of the shielding gas.

The gas regulating valve 20 includes, for example, an electric regulating valve, a pneumatic regulating valve, a hydraulic regulating valve, and the like.

For example, the protective gas is at least one of an inert gas such as helium or argon, and nitrogen.

For example, fig. 2 is a block diagram of an apparatus for co-processing liquid-containing oil sludge by pyrolysis gas condensation according to still another embodiment of the disclosure. As shown in fig. 2, the apparatus for co-processing liquid-containing sludge by pyrolysis gas condensation further includes a condenser 21, and the condenser 21 can cool the oil-water vapor discharged from the first tank 10. The condenser 21 can cool the oil vapor by adopting a direct heat exchange mode or an indirect heat exchange mode, wherein the direct heat exchange mode comprises the step of directly spraying the oil vapor by adopting cooling water; the indirect heat exchange mode comprises cooling oil vapor by adopting a cooling water tube array and the like.

For example, when the indirect heat exchange method is adopted, the condenser 21 is a dividing wall type condenser, the condenser 21 includes a second tank 23, and an accommodating chamber and a cooling medium chamber capable of realizing heat exchange are provided in the second tank 23. The cooling medium flowing in the cooling medium cavity can exchange heat with the oil vapor in the accommodating cavity, so that the oil vapor in the accommodating cavity is cooled.

For example, the second tank 23 further includes a cooling medium inlet and a cooling medium outlet. The cooling medium inlet is communicated with a cooling medium source, and the low-temperature cooling medium is conveyed into the cooling medium cavity. The cooling medium outlet is communicated with the cooling medium cavity, the cooling medium flows in the cooling medium cavity, completes heat exchange with oil-water vapor in the accommodating cavity and then flows out through the cooling medium outlet. After the cooling medium that flows out from the second jar body 23 cools down, is sent back the cooling medium chamber to carry out circulation flow, continuously to holding the interior vapor of oil and water of intracavity and cooling the condensation.

For example, a coil or a plurality of interconnected pipes may be provided in the second tank 23 to allow the cooling medium to flow therethrough. It should be noted that the cooling medium inlet, the cooling medium outlet, and the cooling pipe may refer to a conventional design, and are not limited herein.

For example, as shown in fig. 2, the first tank 10 includes a first exhaust port 22 disposed at the top thereof, the second tank 23 includes a third intake port 24, the first exhaust port 22 is connected to the third intake port 24, and the oil vapor is discharged from the first exhaust port 22 of the first tank 10 and then enters the second tank 23 through the third intake port 24.

For example, the cooling medium chamber is located in the middle of the second tank 23, and the third air inlet 24 and the first drain 27 may be located at the top and the bottom of the second tank 23, respectively, so that the oil-water vapor can flow in from the third air inlet 24 at the top, can flow downward completely, and can be condensed, thereby avoiding the oil-water vapor from being retained at the top of the second tank 23; the first drain port 27 located at the bottom allows the condensed oil-water mixture to be completely drained and prevented from being retained in the second tank 23.

For example, when the direct heat exchange method is adopted, the condenser 21 includes a second tank 23, and the second tank 23 further includes a cooling medium inlet and a cooling medium outlet. The cooling medium may be cooling water or cooling oil, the second tank 23 includes a third air inlet 24, the first air outlet 22 is connected to the third air inlet 24, and the oil vapor is discharged from the first air outlet 22 of the first tank 10 and then enters the second tank 23 through the third air inlet 24. The third air inlet 24 may be located at the lower portion of the second tank 23, and the cooling medium inlet may be located at the upper portion of the second tank 23, so that the cooling medium flows downward and the oil vapor flows upward due to gravity, and the oil vapor can be cooled more sufficiently by the cooling medium.

It should be noted that, as shown in fig. 2, the third air inlet 24 may also be located in the middle of the second tank 23.

For example, as shown in fig. 2, a temperature transmitter 25 is further provided on a pipe connecting the first exhaust port 22 and the third intake port 24, and the liquid phase control valve 16 and the temperature transmitter 25 are interlocked to control the temperature of the oil water vapor discharged from the first exhaust port 22 to 100 ℃ to 200 ℃.

For example, the temperature transmitter 25 can convert the temperature variable of the oil vapor into a transmittable standardized output signal for measurement and control of the oil vapor temperature parameter. When temperature transmitter 25 indicates that the temperature of the oil vapor is below 100 ℃, liquid phase adjustment valve 16 may be instructed to reduce the flow of liquid laden sludge; when the temperature transmitter 25 shows that the temperature of the oil vapor is higher than 200 ℃, the liquid phase regulating valve 16 can be indicated to increase the flow of the liquid-containing oil sludge, so that the interlocking control of the liquid phase regulating valve 16 and the temperature transmitter 25 is realized, and the subsequent oil vapor entering the condenser can be fully utilized.

For example, as shown in fig. 2, the condenser 21 further includes an oil-water separator 26, the second tank 23 includes a first liquid outlet 27 disposed at the bottom thereof, the oil-water separator 26 includes a second liquid inlet 28 disposed at the top thereof, and the first liquid outlet 27 is communicated with the second liquid inlet 28.

It should be noted that, the above mentioned "top" and "bottom" can refer to the similar definitions mentioned above, and are not repeated herein.

For example, the uncondensed gas in the second tank 23 after cooling is purified and used as fuel for the pyrolysis process or sent to a waste furnace for disposal.

For example, at least part of the oil-water vapor in the second tank 23 is condensed to form an oil-water mixture, the temperature of the oil-water mixture is 40 ℃ to 80 ℃, the oil-water mixture is discharged from the first liquid discharge port 27 of the second tank 23, and then enters the oil-water separator 26 from the second liquid inlet 28 communicated with the first liquid discharge port 27. Based on the density difference, the oil-water separator 26 separates the light oil and the oily wastewater in the oil-water mixture discharged from the second tank 23, recovers and reuses the separated light oil, and conveys the separated oily wastewater to the condensation system of the second tank 23 for recycling or discharging into a sewage treatment system.

For example, the condenser 21 can separate the non-condensable gas, the light oil and the water, thereby recovering the light oil and the non-condensable gas in the oil vapor to the maximum extent to improve the oil recovery rate.

For example, as shown in fig. 2, the apparatus for co-processing liquid-containing oil sludge by pyrolysis gas condensation further comprises an oil separator 29, the first tank 10 further comprises a second liquid outlet 30 arranged at the bottom thereof, the oil separator 29 comprises a third liquid inlet 31, and the second liquid outlet 30 is communicated with the third liquid inlet 31. The heavy oil condensed in the first tank 10 can flow down to the second drain port 30 at the bottom to be discharged.

For example, the heated heavy oil and solid phase in the liquid-containing sludge are mixed with the heavy oil condensed from the pyrolysis gas to form a solid-containing oil phase, and the solid-containing oil phase is introduced into the oil separator 29. In the oil separator 29, the solid-oil-containing phase is subjected to sedimentation separation, and the separated heavy oil can be collected by an oil storage tank for further utilization; the separated oil-containing solid phase may be subjected to an advanced treatment to prevent environmental pollution.

For example, the first drain port 22 and the second drain port 30 are respectively located at the top and bottom of the first tank 10, so that the ascending oil-water vapor and the downward heavy oil can completely leave the first tank 10, and the oil can be prevented from being retained in the first tank 10, thereby maximizing the recovery rate of the oil resources.

For example, in the apparatus for the pyrolysis gas condensation cooperative treatment of liquid-containing oil sludge provided by at least one embodiment of the present disclosure, the surface of the pipeline contacting with the outside is covered with an insulating layer, so that the temperature of the medium flowing in the pipeline is kept substantially constant.

For example, the device for the condensation synergistic treatment of the liquid-containing oil sludge by the pyrolysis gas provided by the embodiment of the disclosure can be realized only by the pyrolysis gas and the liquid-containing oil sludge which need to be recycled without adding an external heat source, so that the energy and the resources are utilized to the maximum extent, and the purposes of harmless treatment of the liquid-containing oil sludge and the pyrolysis gas, and recovery of petroleum resources in the pyrolysis gas and the liquid-containing oil sludge to realize resource recycling are achieved. This device of pyrolysis gas condensation coprocessing liquid fatlute can also realize automated control and modular design, and area is little, and the installation is removed conveniently, can handle nearby in the contaminated area to reduce the cost of transportation of liquid fatlute.

At least one embodiment of the present disclosure further provides a method for processing liquid-containing oil sludge by using pyrolysis gas condensation, for example, fig. 3 is a flowchart of processing liquid-containing oil sludge by using pyrolysis gas condensation. As shown in fig. 3, the method includes the following steps.

S01: providing liquid-containing oil sludge and pyrolysis gas;

s02: and contacting the liquid-containing oil sludge with pyrolysis gas for heat exchange so as to condense at least part of an oil phase in the pyrolysis gas, and evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge to obtain oil-water vapor and a solid-containing oil phase.

For example, the temperature of the pyrolysis gas can reach 250 ℃ to 550 ℃, if cooling water, cooling oil and the like are specially adopted to condense the high-temperature pyrolysis gas, the heat of the high-temperature pyrolysis gas cannot be fully utilized, and the consumption of the cooling water or the cooling oil is very large, so that a great deal of resource waste is caused. The liquid-containing oil sludge with high liquid content rate needs to be heated to recover oil resources therein, and meanwhile, environmental pollution can be avoided, so that high-temperature pyrolysis gas is adopted to heat the low-temperature liquid-containing oil sludge, and the low-temperature liquid-containing oil sludge is condensed to the high-temperature pyrolysis gas, so that the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge can be realized, and the resources are utilized to the maximum extent and the environmental pollution can be avoided.

For example, the high-temperature pyrolysis gas is contacted with the low-temperature liquid-containing oil sludge for heat exchange, so that the high-temperature pyrolysis gas can be condensed, and at least part of oil phase in the high-temperature pyrolysis gas is condensed; the liquid-containing oil sludge is heated, so that the water phase and at least part of the oil phase in the liquid-containing oil sludge are evaporated, more oil resources can be recovered under the condition of not increasing energy consumption, the separation of oil and water can be realized under the condition of not using any chemical agent, and the oil resources in the liquid-containing oil sludge are recovered to obtain high-quality oil resources.

For example, the liquid-containing oil sludge is a fluid oil sludge, and the total mass percentage of water and oil in the liquid-containing oil sludge is 70% to 95%. For example, the mass percentage of water and oil in the liquid-containing oil sludge is 70%, 75%, 80%, 85%, 90% or 95%, which can ensure that the liquid-containing oil sludge flows well in the transportation pipeline and can also ensure that the pyrolysis gas is condensed well.

For example, pyrolysis gas is generated by subjecting oil-containing waste to thermal desorption treatment. The thermal desorption process is that under the condition of high temperature and oxygen absence, organic pollutants in the oily waste are subjected to the effects of evaporation, pyrolysis and the like, finally, oil and water in the oily waste are thoroughly separated from a solid phase, and petroleum resources are recycled, so that the harmless treatment and resource utilization of the oily waste are realized. For example, the thermal desorption treatment can be carried out in one or more pyrolysis furnaces, the temperature of the thermal desorption treatment is controlled to be 250-550 ℃, the pyrolysis time is controlled to be 0.4-3.2 h, and the temperature of the finally formed pyrolysis gas is 250-550 ℃. For example, the temperature of the pyrolysis gas is 250 ℃, 300 ℃, 350 ℃, 400 ℃, 450 ℃, 500 ℃ or 550 ℃.

For example, the heavy oil component in the pyrolysis gas condenses into a liquid phase, the stability of the liquid-containing sludge is destroyed by the heating action of the pyrolysis gas, the emulsifiability is reduced, and the water component and the light oil component in the liquid-containing sludge are heated by the pyrolysis gas to form water vapor and oil vapor. The uncondensed gas phase in the pyrolysis gas is mixed with the oil vapor and the water vapor evaporated from the liquid-containing sludge to form oil vapor.

For example, contacting the liquid-containing sludge with pyrolysis gas to exchange heat comprises: and conveying the liquid-containing oil sludge to a liquid inlet of the tank body, conveying the pyrolysis gas to a gas inlet of the tank body, and contacting the liquid-containing oil sludge and the pyrolysis gas in the tank body to perform heat exchange.

For example, fig. 4 is a flow chart of the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge according to still another embodiment of the disclosure, and as shown in fig. 4, the method includes the following steps.

S11: providing liquid-containing oil sludge and pyrolysis gas;

s12: mixing protective gas into the liquid-containing oil sludge during transportation of the liquid-containing oil sludge before contacting the liquid-containing oil sludge with pyrolysis gas;

s13: and contacting the mixture of the liquid-containing oil sludge and the protective gas with pyrolysis gas for heat exchange to condense at least part of an oil phase in the pyrolysis gas, and evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge to obtain oil-water vapor and a solid-containing oil phase.

For example, the shielding gas may prevent the gas volatilized from the liquid-containing sludge or the pyrolysis gas from being oxidized by the oxygen remaining in the tank or the oxygen brought in during the transportation of the liquid-containing sludge under high temperature conditions.

For example, in the process of contacting the mixture of the liquid-containing oil sludge and the protective gas with the pyrolysis gas for heat exchange, the contact area of the liquid-containing oil sludge and the pyrolysis gas can be made larger, so that the heat exchange of the liquid-containing oil sludge and the pyrolysis gas is more sufficient.

For example, fig. 5 is a flow chart of the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge according to another embodiment of the disclosure, and as shown in fig. 5, the method includes the following steps.

S21: providing liquid-containing oil sludge and pyrolysis gas;

s22: conveying the liquid-containing oil sludge and pyrolysis gas, and adjusting the flow of the liquid-containing oil sludge;

s23: and (2) contacting the liquid-containing oil sludge with pyrolysis gas to carry out heat exchange so as to condense at least part of an oil phase in the pyrolysis gas, evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge so as to obtain oil-water vapor and a solid-containing oil phase, and adjusting the flow rate of the liquid-containing oil sludge so as to enable the temperature of the obtained oil-water vapor to be in the range of 100-200 ℃.

For example, during the step of delivering the liquid-containing sludge to the liquid inlet, the flow rate of the liquid-containing sludge is adjusted using at least one of a booster pump and a liquid-phase adjusting valve. For example, the booster pump may be provided on a line carrying the liquid-containing sludge, and the liquid phase regulating valve may be provided between the booster pump and the liquid inlet.

For example, a booster pump may be used to power the flow of the liquid-containing sludge during the transfer of the liquid-containing sludge to the inlet port, i.e. to apply pressure to the liquid-containing sludge to increase the rate of transfer of the liquid-containing sludge to regulate the flow rate of the liquid-containing sludge, and a liquid phase regulating valve may be used to control the opening of the valve to regulate the flow rate of the liquid-containing sludge to ensure that a sufficient amount of the liquid-containing sludge is in sufficient contact with the pyrolysis gas.

For example, a sprayer can be further arranged in the tank body, the sprayer is communicated with the liquid inlet, and the liquid-containing oil sludge can be sprayed to the pyrolysis gas through the sprayer so that the liquid-containing oil sludge is in contact with the pyrolysis gas to perform heat exchange.

For example, fig. 6 is a flow chart of the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge according to another embodiment of the disclosure, and as shown in fig. 6, the method includes the following steps.

S31: providing liquid-containing oil sludge and pyrolysis gas;

s32: conveying the liquid-containing oil sludge to a liquid inlet of the tank body, conveying the liquid-containing oil sludge to a sprayer communicated with the liquid inlet, and conveying the pyrolysis gas to a gas inlet of the tank body;

s33: and spraying the liquid-containing oil sludge to the pyrolysis gas through a sprayer so as to enable the liquid-containing oil sludge to be in contact with the pyrolysis gas for heat exchange, so that at least part of an oil phase in the pyrolysis gas is condensed, and at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge are evaporated so as to obtain oil-water vapor and a solid-containing oil phase.

For example, the tank further includes an exhaust port for discharging oil vapor, a temperature transmitter is provided in the transfer passage from which the oil vapor is discharged, and the method further includes: the temperature of the oil vapor is controlled between 100 ℃ and 200 ℃ through the interlocking control of the temperature transmitter and the liquid phase regulating valve.

For example, fig. 7 is a flow chart of the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge according to another embodiment of the disclosure, and as shown in fig. 7, the method includes the following steps.

S41: providing liquid-containing oil sludge and pyrolysis gas;

s42: conveying the liquid-containing oil sludge and pyrolysis gas, and adjusting the flow of the liquid-containing oil sludge;

s43: contacting the liquid-containing oil sludge with pyrolysis gas to carry out heat exchange so as to condense at least part of oil phase in the pyrolysis gas, evaporating at least part of water phase and at least part of oil phase in the liquid-containing oil sludge so as to obtain oil-water vapor and solid-containing oil phase, and controlling the temperature of the oil-water vapor to be between 100 and 200 ℃ through the interlocking control of a temperature transmitter and a liquid phase regulating valve.

For example, the temperature transmitter may convert the temperature variable of the oil vapor into a transmittable normalized output signal for measurement and control of the oil vapor temperature parameter. When the temperature transmitter displays that the temperature of the oil vapor is lower than 100 ℃, the liquid phase regulating valve can be indicated to reduce the flow of the liquid-containing oil sludge; when the temperature transmitter displays that the temperature of the oil vapor is higher than 200 ℃, the liquid phase regulating valve can be indicated to increase the flow of the liquid-containing oil sludge so as to realize the interlocking control of the liquid phase regulating valve and the temperature transmitter, so that the subsequent oil vapor entering the condenser can be fully utilized.

For example, fig. 8 is a flow chart of the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge according to another embodiment of the disclosure, and as shown in fig. 8, the method includes the following steps.

S51: providing liquid-containing oil sludge and pyrolysis gas;

s52: contacting the liquid-containing oil sludge with pyrolysis gas for heat exchange so as to condense at least part of an oil phase in the pyrolysis gas, and evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge to obtain oil-water vapor and a solid-containing oil phase;

s53: condensing the oil-water vapor to obtain an oil-water mixture and a non-condensable gas;

s54: carrying out oil-water separation on the oil-water mixture to obtain light oil and oily wastewater, and collecting non-condensable gas;

s55: and settling and separating the solid oil-containing phase to obtain heavy oil and an oil-containing solid phase.

For example, when the process is completed in the apparatus for co-processing liquid-containing oil sludge by pyrolysis gas condensation as shown in fig. 2, the method for co-processing liquid-containing oil sludge by pyrolysis gas condensation comprises condensing oil water vapor by using a condenser, wherein the condenser comprises a second tank and an oil-water separator, conveying the oil water vapor to the second tank, and cooling the oil water vapor to 40-80 ℃ in the second tank to obtain an oil-water mixture and non-condensable gas; conveying the oil-water mixture to an oil-water separator to obtain light oil and oily wastewater; while the non-condensable gases are collected.

For example, cooling the oil-water vapor in the second tank includes cooling the oil-water vapor by direct heat exchange or indirect heat exchange, and the direct heat exchange includes directly spraying the oil-water vapor by oil or water; the indirect heat exchange mode comprises cooling oil vapor by adopting a cooling water tube array and the like.

For example, the oil-water separator separates light oil and oily wastewater in an oil-water mixture discharged from the second tank based on the density difference, recovers and reuses the separated light oil, and conveys the separated oily wastewater to a condensation system of the second tank for recycling or discharging into a sewage treatment system. The condenser can separate non-condensable gas, light oil and water, so that the oil in oil vapor is recovered to the maximum extent, and the recovery rate of oil resources is improved.

For example, the method for the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge further comprises the steps of performing sedimentation separation on heavy oil and an oil-containing solid phase by using an oil separator, wherein the separated heavy oil can be collected by using an oil storage tank for further utilization; the separated oil-containing solid phase is subjected to advanced treatment.

For example, fig. 9 is a flow chart of the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge according to another embodiment of the disclosure. For example, the method for the pyrolysis gas condensation co-processing of the liquid-containing oil sludge shown in fig. 9 is implemented in the apparatus for the pyrolysis gas condensation co-processing of the liquid-containing oil sludge shown in fig. 2. As shown in fig. 9, the method includes the following steps.

S61: providing liquid-containing oil sludge, pyrolysis gas and protective gas;

s62: conveying the pyrolysis gas to a first gas inlet of the first tank;

s63: applying pressure to the liquid-containing oil sludge by using a booster pump, adjusting the flow of the liquid-containing oil sludge by using a liquid-phase adjusting valve, and conveying the liquid-containing oil sludge to a first liquid inlet of a first tank body;

s64: protective gas is input from the second gas inlet and is transmitted between the sprayer and the first liquid inlet;

s65: mixing the liquid-containing oil sludge with protective gas, and conveying the mixed liquid-containing oil sludge and protective gas to a sprayer;

s66: and spraying the mixture of the liquid-containing oil sludge and the protective gas to the pyrolysis gas by using a sprayer, enabling the liquid-containing oil sludge to contact with the pyrolysis gas to carry out heat exchange so as to condense at least part of an oil phase in the pyrolysis gas, and evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge so as to obtain oil-water vapor and a solid-containing oil phase.

For example, the method for the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge further comprises the following steps: the method comprises the following steps of spraying liquid-containing oil sludge to pyrolysis gas by using a sprayer 17 positioned in a first tank body 10, wherein the sprayer 17 is communicated with a first liquid inlet 11, the first liquid inlet 11 and the sprayer 17 are positioned at the upper part of the first tank body 10, and a first air inlet 12 is positioned at the lower part of the first tank body 10.

For example, the first tank 10 further includes a second gas inlet 19 at the top thereof, the second gas inlet 19 is communicated between the sprayer 17 and the first liquid inlet 11, and the protective gas and the liquid-containing sludge entering from the second gas inlet 19 are mixed and then conveyed to the sprayer 17. The second air inlet 19 is positioned at the top of the first tank body 10, so that the second air inlet 19 is communicated between the sprayer 17 and the first liquid inlet 11, the length of a pipeline positioned in the first tank body 10 can be reduced, and meanwhile, the downward flowing of the protective gas is facilitated to be directly mixed with the liquid-containing mud.

For example, the shielding gas is transmitted through a third pipeline 18 extending to and communicating with the second gas inlet 19, and a gas regulating valve 20 is further provided on the third pipeline 18, and the flow rate of the shielding gas can be regulated by using the gas regulating valve 20. For example, the opening of the valve of the gas regulating valve 20 can be automatically controlled according to the signal of the regulating part, thereby realizing the regulation of the flow rate of the shielding gas.

For example, fig. 10 is a flow chart of the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge according to another embodiment of the disclosure. For example, the method for the pyrolysis gas condensation co-processing of the liquid-containing oil sludge shown in fig. 10 is implemented in the apparatus for the pyrolysis gas condensation co-processing of the liquid-containing oil sludge shown in fig. 2. As shown in fig. 10, the method includes the following steps.

S71: providing liquid-containing oil sludge, pyrolysis gas and protective gas;

s72: conveying the pyrolysis gas to a first gas inlet of the first tank;

s73: applying pressure to the liquid-containing oil sludge by using a booster pump, adjusting the flow of the liquid-containing oil sludge by using a liquid-phase adjusting valve, and conveying the liquid-containing oil sludge to a first liquid inlet of a first tank body;

s74: protective gas is input from the second gas inlet, the protective gas is transmitted between the sprayer and the first liquid inlet, the liquid-containing oil sludge and the protective gas are mixed, and the mixed liquid-containing oil sludge and the mixed protective gas are transmitted to the sprayer;

s75: spraying a mixture of liquid-containing oil sludge and protective gas to the pyrolysis gas by using a sprayer, enabling the liquid-containing oil sludge to contact with the pyrolysis gas to carry out heat exchange so as to condense at least part of an oil phase in the pyrolysis gas, and evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge so as to obtain oil-water vapor and a solid-containing oil phase;

s76: the temperature of oil-water vapor is controlled between 100 ℃ and 200 ℃ through the interlocking control of a temperature transmitter and a liquid phase regulating valve between a first exhaust port of a first tank body and a third air inlet of a second tank body, wherein the third air inlet is arranged between the first exhaust port of the first tank body and a condenser;

s77: the oil-water vapor is transmitted from the first exhaust port to the third air inlet to enter the second tank body, the oil-water vapor is cooled to 40-80 ℃ to obtain an oil-water mixture and non-condensable gas, the non-condensable gas is collected, and the oil-water mixture is conveyed to an oil-water separator which is arranged in a condenser;

s78: separating the light oil and the oily wastewater in an oil-water separator based on the density difference;

s79: and discharging the solid-oil-containing phase from a second liquid outlet positioned at the bottom of the first tank body, conveying the solid-oil-containing phase to an oil separator, and separating heavy oil and an oil-containing solid phase in a settling separation mode.

For example, the apparatus for the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge further comprises a condenser 21, the first tank 10 further comprises a first exhaust port 22 at the top thereof, and the oil-water vapor is discharged from the first exhaust port 22 to the condenser 21; the condenser 21 comprises a second tank 23, the second tank 23 comprises a third air inlet 24, and the first exhaust port 22 is communicated with the third air inlet 24; the temperature of the oil vapor is controlled to be 100 to 200 ℃ by the interlocking control of the temperature transmitter 25 and the liquid phase regulating valve 16 between the first exhaust port 22 and the third intake port 24.

For example, the method for the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge further comprises the following steps: conveying the oil-water vapor to a second tank 23, and cooling the oil-water vapor to 40-80 ℃ in the second tank 23 to obtain an oil-water mixture and non-condensable gas; the oil-water mixture is sent to an oil-water separator 26 included in the condenser 21 to obtain light oil and oily wastewater; while the non-condensable gases are collected.

For example, cooling the oil-water vapor in the second tank 23 includes cooling the oil-water vapor by direct heat exchange or indirect heat exchange, and the direct heat exchange includes directly spraying the oil-water vapor by oil or water; the indirect heat exchange mode comprises cooling oil vapor by adopting a cooling water tube array and the like.

For example, when the indirect heat exchange method is adopted, the condenser 21 used is a dividing wall type condenser, the dividing wall type condenser 21 includes a second tank 23, and a receiving chamber and a cooling medium chamber capable of performing heat exchange are provided in the second tank 23. The cooling medium flowing in the cooling medium cavity can exchange heat with the gas in the accommodating cavity, so that the oil vapor in the accommodating cavity is cooled.

For example, the second tank 23 further includes a cooling medium inlet and a cooling medium outlet. The cooling medium inlet is communicated with a cooling medium source, and the low-temperature cooling medium is conveyed into the cooling medium cavity. The cooling medium outlet is communicated with the cooling medium cavity, the cooling medium flows in the cooling medium cavity, completes heat exchange with oil-water vapor in the accommodating cavity and then flows out through the cooling medium outlet. After the cooling medium that flows out from the second jar of body 23 cools down, is sent back the cooling medium chamber to carry out the circulation and flow, the oil vapor that lasts to holding the intracavity cools down the condensation.

For example, the first tank 10 includes a first exhaust port 22 disposed at the top thereof, the second tank 23 includes a third intake port 24, the first exhaust port 22 is connected to the third intake port 24, and the oil vapor is discharged from the first exhaust port 22 of the first tank 10 and then enters the second tank 23 through the third intake port 24.

For example, the cooling medium chamber is located in the middle of the second tank 23, and the third air inlet 24 and the first liquid outlet 27 may be located at the top and the bottom of the second tank 23, respectively, so that the oil-water vapor can flow in from the third air inlet 24 at the top, can flow downward completely, and can be condensed, thereby avoiding the oil-water vapor from being retained at the top of the second tank 23; the first drain port 27 at the bottom allows the condensed oil-water mixture to be completely drained and prevented from staying in the second tank 23.

For example, when the direct heat exchange method is adopted, the condenser 21 includes a second tank 23, and the second tank 23 further includes a cooling medium inlet and a cooling medium outlet. The cooling medium can be water or oil, the second tank 23 comprises a third air inlet 24, the first air outlet 22 is connected with the third air inlet 24, and the oil vapor is discharged from the first air outlet 22 of the first tank 10 and then enters the second tank 23 from the third air inlet 24. The third air inlet 24 may be located at the lower portion of the second tank 23, and the cooling medium inlet may be located at the upper portion of the second tank 23, so that the cooling medium flows downward and the oil vapor flows upward due to gravity, and the oil vapor can be cooled more sufficiently by the cooling medium.

For example, the oil-water separator 26 separates light oil and oily wastewater in the oil-water mixture discharged from the second tank 23 based on the density difference, recovers and reuses the separated light oil, and transfers the separated oily wastewater to the condensation system of the second tank 23 for recycling or discharge into a wastewater treatment system.

For example, the condenser 21 can separate the non-condensable gas, the light oil and the water, thereby recovering the crude oil in the oil vapor to the maximum extent to improve the recovery rate of the oil resource.

For example, the method for the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge further comprises the following steps: the solid-oil-containing phase is discharged from a second liquid discharge port 30 located at the bottom of the first tank 10, and is sent to an oil separator 29 to settle and separate the heavy oil and the solid oil-containing phase.

For example, the oil separator 29 includes a third liquid inlet 31, and the second liquid discharge port 30 communicates with the third liquid inlet 31. The solid-containing oil phase formed by the heated heavy oil and solid phase in the liquid-containing sludge mixed with the heavy oil condensed from the pyrolysis gas can flow down to the second drain 30 at the bottom for discharge into the oil separator 29. In the oil separator 29, the solid-oil-containing phase is subjected to sedimentation separation, and the separated heavy oil can be collected by an oil storage tank for further utilization; the separated oil-containing solid phase is subjected to advanced treatment.

For example, the first drain port 22 and the second drain port 30 are located at the top and bottom of the first tank 10, respectively, so that the ascending oil-water vapor and the descending heavy oil can completely leave the first tank 10 and can be prevented from staying in the first tank 10.

The device and the method for the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge have at least one of the following beneficial effects:

(1) according to the method for the condensation and synergistic treatment of the liquid-containing oil sludge by the pyrolysis gas, the high-temperature pyrolysis gas is contacted with the liquid-containing oil sludge to exchange heat, so that the liquid-containing oil sludge condenses the high-temperature pyrolysis gas, the high-temperature pyrolysis gas heats the liquid-containing oil sludge, at least part of oil phase in the high-temperature pyrolysis gas is condensed, and at least part of oil phase in the liquid-containing oil sludge volatilizes, so that resources are saved.

(2) According to the method for the pyrolysis gas condensation synergistic treatment of the liquid-containing oil sludge, provided by at least one embodiment of the disclosure, the separation of oil and water is realized without using any chemical agent and increasing additional energy consumption, and more oil resources are recovered.

(3) According to the method for the condensation and cooperative treatment of the liquid-containing oil sludge by the pyrolysis gas, which is provided by at least one embodiment of the disclosure, the protective gas and the liquid-containing oil sludge form a mixture and then are conveyed to the sprayer, so that the contact area of the liquid-containing oil sludge and the pyrolysis gas is larger during spraying, and the heat exchange between the liquid-containing oil sludge and the pyrolysis gas is more sufficient.

(4) The device of pyrolysis gas condensation coprocessing liquid-containing oil sludge that this at least embodiment of disclosure provided, for first air inlet, first inlet is more close to the top of first jar of body for liquid-containing oil sludge flows to the direction of keeping away from the top under the effect of gravity, and pyrolysis gas flows to the direction that is close to the top, makes pyrolysis gas and the surface of liquid-containing oil sludge contact more, thereby makes liquid-containing oil sludge and pyrolysis gas contact more abundant, and the process of heat exchange is also more abundant.

(5) According to the device for the pyrolysis gas condensation cooperative treatment of the liquid-containing oil sludge, the liquid phase regulating valve and the temperature transmitter are controlled in an interlocking manner, the temperature of oil-water vapor discharged from the first exhaust port is controlled to be 100-200 ℃, so that the oil-water vapor can be fully condensed after entering the condenser, and the oil-water vapor entering the condenser can be fully utilized.

The following points need to be explained:

(1) the drawings of the embodiments of the invention only relate to the structures related to the embodiments of the invention, and other structures can refer to common designs.

(2) The thickness of layers or regions in the figures used to describe embodiments of the invention may be exaggerated or reduced for clarity, i.e., the figures are not drawn on a true scale. It will be understood that when an element such as a layer, film, region, or substrate is referred to as being "on" or "under" another element, it can be "directly on" or "under" the other element or intervening elements may be present.

(3) Without conflict, embodiments of the present invention and features of the embodiments may be combined with each other to arrive at new embodiments.

The above description is only an embodiment of the present invention, but the scope of the present invention is not limited thereto, and the scope of the present invention should be subject to the scope of the claims.

Claims

1. A method for the condensation and cooperative treatment of liquid-containing oil sludge by pyrolysis gas comprises the following steps:

providing liquid-containing oil sludge and pyrolysis gas;

and contacting the liquid-containing oil sludge with the pyrolysis gas for heat exchange so as to condense at least part of an oil phase in the pyrolysis gas, and evaporating at least part of a water phase and at least part of an oil phase in the liquid-containing oil sludge to obtain oil-water vapor and a solid-containing oil phase.

2. The method of claim 1 wherein a shielding gas is mixed into the liquid-containing sludge prior to contacting the liquid-containing sludge with the pygas.

3. The method according to claim 1, wherein the flow rate of the liquid-containing sludge is adjusted so that the temperature of the obtained oil-water vapor is in the range of 100 ℃ to 200 ℃.

4. The process of any one of claims 1-3, wherein contacting the liquid-containing sludge in heat exchange with the pygas comprises:

and conveying the liquid-containing oil sludge to a liquid inlet of a tank body, conveying the pyrolysis gas to a gas inlet of the tank body, and contacting the liquid-containing oil sludge and the pyrolysis gas in the tank body to perform heat exchange.

5. The method according to claim 4, wherein a sprayer is arranged in the tank, the sprayer is communicated with the liquid inlet, and the liquid-containing oil sludge is sprayed to the pyrolysis gas through the sprayer so as to contact the liquid-containing oil sludge with the pyrolysis gas for heat exchange.

6. The method of claim 4, wherein the flow rate of the liquid-containing sludge is regulated during the delivery of the liquid-containing sludge to the liquid inlet using at least one of a booster pump and a liquid phase regulating valve.

7. The method of claim 6, wherein,

the tank body further comprises an exhaust port for discharging the oil-water vapor, a temperature transmitter is arranged in a conveying passage for discharging the oil-water vapor from the exhaust port, and the method further comprises the following steps:

and the temperature of the oil vapor is controlled to be between 100 and 200 ℃ through the interlocking control of the temperature transmitter and the liquid phase regulating valve.

8. The method of any of claims 1-3, further comprising:

condensing the oil-water vapor to obtain an oil-water mixture and a non-condensable gas;

carrying out oil-water separation on the oil-water mixture to obtain light oil and oily wastewater; and

and collecting the non-condensable gas.

9. The method of any of claims 1-3, further comprising:

and settling and separating the solid oil-containing phase to obtain heavy oil and an oil-containing solid phase.

10. A device for the condensation and cooperative treatment of liquid-containing oil sludge by pyrolysis gas comprises:

the first tank comprises a first liquid inlet and a first air inlet;

a first conduit in communication with a source of liquid-containing sludge and extending to the first inlet;

a second pipeline communicated with a pyrolysis gas source and extending to the first gas inlet;

wherein the first conduit is configured to convey liquid-containing sludge derived from the source of liquid-containing sludge to the first inlet port, the second conduit is configured to convey pyrolysis gas derived from the source of pyrolysis gas to the first inlet port, and the liquid-containing sludge and the pyrolysis gas are contacted in the first tank for heat exchange.

11. The apparatus according to claim 10 for the cooperative processing of liquid-containing sludge by pyrolysis gas condensation, further comprising: the liquid phase regulating valve is arranged between the booster pump and the first liquid inlet.

12. The apparatus for the cooperative condensation treatment of liquid-containing sludge according to claim 10 or 11, further comprising a sprayer disposed in the first tank, wherein the sprayer is in communication with the first liquid inlet, the first liquid inlet and the sprayer are disposed at an upper portion of the first tank, and the first gas inlet is disposed at a lower portion of the first tank.

13. The apparatus for the cooperative processing of liquid-containing sludge by pyrolysis gas condensation according to claim 12 wherein the spray header comprises a plurality of spray headers arranged in one or more rows.

14. The apparatus according to claim 12 for the cooperative processing of liquid-containing sludge by pyrolysis gas condensation, further comprising a third conduit in communication with a source of shielding gas, wherein the first tank further comprises a second gas inlet at a top thereof, and the third conduit extends to the second gas inlet.

15. The apparatus according to claim 14 wherein the second gas inlet is connected between the sparger and the first liquid inlet so that the shielding gas and the liquid-containing sludge are mixed and then delivered to the sparger.

16. The apparatus according to claim 15 wherein the first tank includes a first exhaust port disposed at a top portion thereof, the condenser includes a second tank including a third inlet port, and the first exhaust port is connected to the third inlet port.

17. The apparatus for co-processing liquid-containing oil sludge by pyrolysis gas condensation according to claim 16, wherein a temperature transmitter is arranged on a pipeline connecting the first exhaust port and the third inlet port, and the liquid phase regulating valve and the temperature transmitter are controlled in an interlocking manner to control the temperature of oil-water vapor discharged from the first exhaust port to be 100-200 ℃.

18. The apparatus according to claim 17, wherein the condenser further comprises a water-oil separator, the second tank comprises a first liquid outlet at the bottom thereof, the water-oil separator comprises a second liquid inlet at the top thereof, and the first liquid outlet is communicated with the second liquid inlet.

19. The apparatus for the cooperative processing of liquid-containing sludge by the condensation of pyrolysis gas according to any one of claims 16 to 18, further comprising an oil separator, wherein the first tank further comprises a second liquid outlet disposed at the bottom thereof, and the oil separator comprises a third liquid inlet, and the second liquid outlet is communicated with the third liquid inlet.