CN209957707U - Oil-containing pollutant sequential batch continuous treatment system - Google Patents

Abstract

The utility model discloses a continuous processing system for oil-containing pollutants in sequence batch, which comprises more than two intermittent reduced pressure distillation devices and a continuous pyrolysis device, wherein the feed inlet of the continuous pyrolysis device is respectively connected with the heavy phase outlets of the intermittent reduced pressure distillation devices; and the continuous pyrolysis device continuously receives the heavy components from the batch type reduced pressure distillation device and processes the heavy components to obtain pyrolysis oil and residues. The utility model provides a continuous processing system is criticized to oily pollutant preface has higher suitability to oily pollutant, and the stability and the security of processing procedure are higher to higher treatment effeciency and oil content recovery efficiency have.

Description

Oil-containing pollutant sequential batch continuous treatment system

Technical Field

The utility model relates to an oily pollutant handles technical field, especially relates to an oily pollutant preface batch continuous processing system.

Background

In the exploration, exploitation, storage and transportation and refining processes of petroleum, a large amount of oil-containing pollutants can be generated, and from the source, the oil-containing solid waste generated in the exploitation of crude oil, the oil-containing solid waste generated in the gathering and transportation process of an oil field and the oil-containing solid waste generated in the sewage treatment of an oil refinery can be included. The oil-containing pollutants have different forms and compositions, usually have an oil content of 10-50% and a water content of 40-90%, and also contain impurities of various forms and contents. If the oily pollutants cannot be effectively treated, the oily pollutants can seriously damage the ecological environment and form serious threats to human health. However, the existing oily pollutant treatment device has high requirements on feeding oily pollutants and low adaptability to oily pollutants of different sources.

SUMMERY OF THE UTILITY MODEL

The embodiment of the utility model provides a continuous processing system is criticized to oily pollutant preface, aim at improves the suitability to oily pollutant to improve oily pollutant's treatment effeciency.

The embodiment of the utility model provides a continuous type processing system is criticized to oily pollutant preface, the system includes: the device comprises more than two intermittent reduced pressure distillation devices, wherein each intermittent reduced pressure distillation device comprises a first chamber, and a first feed inlet, a gas phase outlet and a heavy phase outlet which are communicated with the first chamber; continuous type pyrolysis device, continuous type pyrolysis device include the second cavity and with the second feed inlet, pyrolysis gas export and the residue export of second cavity intercommunication, the second feed inlet respectively with two above intermittent type formula vacuum distillation plant's heavy phase exit linkage, continuous type pyrolysis device receives heavy component in succession and handles and obtain pyrolysis oil content and residue.

The embodiment of the utility model provides an oily pollutant preface batch continuous processing system, the heavy phase export of two above intermittent type formula vacuum distillation apparatus is connected with continuous type pyrolysis device's feed inlet respectively through the valve, divide into two above batches with oily pollutant and send into two above intermittent type formula vacuum distillation apparatus respectively, two above intermittent type formula vacuum distillation apparatus carry out intermittent type formula vacuum distillation to oily pollutant separately and handle and obtain light oil content and heavy component, owing to adopt intermittent type formula vacuum distillation operation, to the form of oily pollutant, constitute, the moisture content, the form of impurity, impurity rate and oiliness rate etc. all have no special requirement, adaptability to oily pollutant is higher, can handle the oily pollutant of various sources; the two or more intermittent reduced pressure distillation devices send out heavy components in batches according to a preset sequence, so that the heavy components are continuously provided for the continuous pyrolysis device, and the continuous pyrolysis device continuously receives the heavy components and processes the heavy components to obtain pyrolysis oil and residues, so that the treatment system has high treatment efficiency and is suitable for treating large-batch oil-containing pollutants.

In addition, because the intermittent reduced pressure distillation device removes the water in the oily pollutant and recovers a large amount of oil in the oily pollutant, the oil content of the obtained heavy component is obviously reduced, the disturbance of the water is avoided in the treatment process of the continuous pyrolysis device, the process stability is higher, the recovery rate of the oil in the oily pollutant is improved, the treatment efficiency is further improved, and the energy consumption of the continuous pyrolysis device is obviously reduced.

Because of the adoption of the intermittent reduced pressure distillation operation, the intermittent reduced pressure distillation device has good tightness in the operation process, greatly reduces the distillation operation temperature, has balanced internal pressure and convenient control, prevents air leakage, and ensures lower oxygen content and higher vacuum degree in the device, thereby ensuring higher stability and safety in the operation process of the intermittent reduced pressure distillation device, improving the recovery efficiency of light oil content, saving energy and reducing consumption.

Adopt the utility model provides an oily pollutant preface batch continuous processing system, higher suitability has to various oily pollutants, realized the innocent treatment to the oily pollutant of various sources well, oil content recovery efficiency is high, total petroleum hydrocarbon content is below 0.3 wt% in the residue that obtains, main pollutant emission index reaches and is superior to "oil refining industry pollutant emission standard" (GB31570-2015) even, satisfy strict environmental protection requirement, and have higher treatment effeciency, the process stability and security are higher, can also the energy saving, reduce the energy consumption.

Drawings

In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required to be used in the embodiments of the present invention will be briefly described below, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.

Fig. 1 is a schematic structural diagram of a sequential batch continuous treatment system for oily pollutants according to an embodiment of the present invention.

Fig. 2 is a schematic flow chart of a sequential batch continuous treatment method for oily pollutants according to an embodiment of the present invention.

Fig. 3 is a schematic flow chart of a sequential batch continuous treatment method for oily pollutants according to an embodiment of the present invention.

Detailed Description

The features and exemplary embodiments of various aspects of the present invention will be described in detail below, and in order to make the objects, technical solutions, and advantages of the present invention more apparent, the present invention will be further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention. It will be apparent to one skilled in the art that the present invention may be practiced without some of these specific details. The following description of the embodiments is merely intended to provide a better understanding of the invention by illustrating examples of the invention.

It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.

First, a sequential batch continuous treatment system for oily pollutants according to an embodiment of the present invention will be described in detail with reference to fig. 1.

Fig. 1 is a schematic structural diagram of a sequential batch continuous treatment system for oily pollutants according to an embodiment of the present invention. Referring to fig. 1, a sequential batch continuous treatment system for oily pollutants according to an embodiment of the present invention includes more than two batch vacuum distillation apparatuses 1 and a continuous pyrolysis apparatus 2 connected to the more than two batch vacuum distillation apparatuses 1.

The batch type reduced pressure distillation device 1 comprises a first chamber 101, and a first feed inlet 102, a gas phase outlet 103 and a heavy phase outlet 104 which are communicated with the first chamber 101, wherein the first feed inlet 102 is provided with a valve 3a, and the heavy phase outlet 104 is provided with a valve 3 b. The intermittent reduced pressure distillation device 1 is used for performing intermittent reduced pressure distillation treatment on oil-containing pollutants to obtain light oil components and heavy components, and the heavy components are discharged by the intermittent reduced pressure distillation device 1 according to a preset sequence in batches.

The continuous pyrolysis device 2 comprises a second chamber 201, and a second feed inlet 202, a pyrolysis gas outlet 203 and a residue outlet 204 which are communicated with the second chamber 201, wherein the second feed inlet 202 is respectively connected with the heavy phase outlets 104 of the more than two batch-type reduced pressure distillation devices 1, and the continuous pyrolysis device 2 continuously receives heavy components and processes the heavy components to obtain pyrolysis oil and residues.

According to the utility model discloses oily pollutant preface batch continuous processing system, divide into the oily pollutant of pending two above batches and send into more than two intermittent type formula vacuum distillation device 1 respectively, close the valve 3a of first feed inlet 102 and the valve 3b of heavy phase export 104, intermittent type formula vacuum distillation device 1 carries out intermittent type formula vacuum distillation processing to oily pollutant under airtight, the condition of decompression, obtains light oil content and heavy component. Because of the adoption of the intermittent reduced pressure distillation operation, the device has no special requirements on the shape, the composition, the water content, the shape of the contained impurities, the impurity rate, the oil content and the like of the oily pollutants to be treated, has higher adaptability to the oily pollutants and can treat the oily pollutants from various sources.

Because of the adoption of the intermittent reduced pressure distillation operation, the intermittent reduced pressure distillation device 1 has good tightness in the operation process, greatly reduces the distillation operation temperature, has balanced internal pressure and convenient control, prevents air leakage, and ensures lower oxygen content and higher vacuum degree in the device, thereby ensuring that the intermittent reduced pressure distillation device 1 has higher stability and safety in the operation process, improving the recovery efficiency of light oil, saving energy and reducing consumption.

The two or more intermittent reduced pressure distillation devices 1 send out heavy components in batches according to a preset sequence, so that the heavy components are continuously provided for the continuous pyrolysis device 2, the continuous pyrolysis device 2 continuously receives the heavy components, and the heavy components are pyrolyzed to obtain pyrolysis oil and residues, so that the treatment system has high treatment efficiency and is suitable for treating large-batch oil-containing pollutants.

Because the water in the oily pollutant is removed in the intermittent reduced pressure distillation device 1 and a large amount of oil in the oily pollutant is recovered, the oil content in the obtained heavy component is obviously reduced, the disturbance of the water to the treatment process is avoided in the treatment process of the continuous pyrolysis device 2, the process stability is higher, the oil recovery rate in the oily pollutant is improved, the treatment efficiency is further improved, and the energy consumption of the continuous pyrolysis device 2 is obviously reduced.

It is understood that the number of the batch type vacuum distillation apparatuses 1 may be two, three, four, etc. The batch vacuum distillation apparatus 1 can regulate and control the operation of more than two batch vacuum distillation apparatuses 1 according to the actual treatment requirement, as long as the requirement of continuously supplying heavy components to the continuous pyrolysis apparatus 2 is met. For example, the oil-containing pollutant is divided into two or more batches and is respectively sent to two or more batch type reduced pressure distillation devices 1 according to a preset time interval, and the two or more batch type reduced pressure distillation devices 1 enter a reduced pressure distillation process according to a preset time interval so as to realize the batch sending of the heavy component according to a preset sequence, thereby continuously providing the heavy component to the continuous pyrolysis device 2.

In some embodiments, the heavy phase outlets 104 of two or more batch vacuum distillation apparatuses 1 are connected to the second feed port 202 of the continuous pyrolysis apparatus 2 through the first storage apparatus 4. The first storage device 4 is used for buffering heavy components from the batch type reduced pressure distillation device 1, so that the batch type reduced pressure distillation device 1 can independently discharge materials, and the continuous type pyrolysis device 2 can independently feed materials, so that the system can run more stably.

As an example, the number of the batch type reduced pressure distillation apparatuses 1 is two, and they are referred to as a first batch type reduced pressure distillation apparatus and a second batch type reduced pressure distillation apparatus, respectively. After the first intermittent reduced pressure distillation device finishes feeding, closing a valve 3a of a first feeding hole 102, starting temperature rise, and performing a reduced pressure distillation process, at the moment, finishing the reduced pressure distillation process by a second intermittent reduced pressure distillation device, opening a valve 3b of a heavy phase outlet 104, performing a discharging process, discharging heavy components into a first storage device 4, after discharging, closing the valve 3b of the heavy phase outlet 104, opening the valve 3a of the first feeding hole 102, performing a feeding process, and then entering a low-temperature constant-temperature waiting process, after the reduced pressure distillation process is finished by the first intermittent reduced pressure distillation device, heating the second intermittent reduced pressure distillation device, starting the reduced pressure distillation process, and sequentially performing the discharging process, the feeding process and the low-temperature constant-temperature waiting process by the first intermittent reduced pressure distillation device, and sequentially circulating according to the above sequence. The first batch type reduced pressure distillation device and the second batch type reduced pressure distillation device operate alternately, so that sequencing batch type continuous operation is formed, and the treatment efficiency of batch type reduced pressure distillation is improved.

Further, the vacuum distillation step may include: heating the oil-containing pollutants from the normal temperature to 50 ℃ to 150-180 ℃ at a preset heating rate under the absolute pressure of below 50kPa for reduced pressure distillation and dehydration; and then, under the absolute pressure of below 50kPa, gradually heating the dehydrated oily pollutant from 150-180 ℃ to 370-400 ℃ according to a preset heating rate to carry out reduced pressure distillation treatment, gradually gasifying the light oil component to separate from the oily pollutant along with the temperature rise, and recovering the light oil component after condensation liquefaction, wherein the light oil component contains gasoline, diesel oil, lubricating oil and the like, and the residue is a heavy component.

In the vacuum distillation process, after moisture of the oily pollutants is removed, the light oil content is recovered by vacuum distillation, so that the disturbance of moisture to the vacuum distillation process is avoided, the process stability is improved, the moisture content of the oily sludge incoming material is not limited, the oily pollutants with any moisture content can be treated, the applicability to various oily pollutants is improved, the quality and the recovery rate of the light oil content are improved, and the energy conservation and consumption reduction are facilitated.

In the vacuum distillation process, the proper operation temperature and heating rate can be determined according to the difference of the compositions of oil-containing pollutants from different sources.

For example, in the vacuum distillation step, the oil-containing contaminant is gradually heated from 50 ℃ to 180 ℃ under an absolute pressure of 50kPa or less to be subjected to vacuum distillation dehydration, then the temperature is gradually increased from 180 ℃ to 370 ℃ to volatilize and separate the light oil component in the oil-containing contaminant, and after the separated gaseous water and light oil component are condensed and liquefied, the water and light oil component can be respectively recovered according to different distillation temperatures and different components. The operating temperature of the reduced pressure distillation process is reduced, and energy conservation and consumption reduction are realized.

Further, the batch type reduced pressure distillation apparatus 1 further comprises a stirring component and a first heating component. The stirring assembly is arranged in the first chamber 101 and is used for stirring the oil-containing pollutants; a first heating assembly is disposed around the first chamber 101 for heating the oil-containing contaminants. Can conveniently realize the heating to the oily pollutant through first heating element, stir oily pollutant through stirring subassembly, guarantee to the even, high-efficient, quick transmission heat of oily pollutant, improve the recovery efficiency to light oil content among the oily pollutant to energy saving and consumption reduction.

In some embodiments, the batch vacuum distillation apparatus 1 is a horizontal reaction kettle with horizontal stirring, the shell includes an inner shell 105 and an outer shell 106, which are sleeved with each other, an inner wall surface of the inner shell 105 encloses to form a first chamber 101, the first feed inlet 102, the gas phase outlet 102 and the heavy phase outlet 103 respectively penetrate through the inner shell 105 and the outer shell 106 and are communicated with the first chamber 101, the heavy phase outlet 104 is located at the bottom of the shell, and the first feed inlet 102 and the gas phase outlet 103 are separately located at two ends of the top of the shell.

The stirring assembly comprises a stirring shaft 107, stirring blades 108 connected to the stirring shaft 107, and a driving part 109 for driving the stirring shaft 107 to rotate relative to the casing. The axis of the stirring shaft 107 is aligned with the central line of the first chamber 101, two opposite ends of the stirring shaft 107 are respectively rotatably connected to two corresponding ends of the housing, for example, rotatably connected by a bearing, and any one of the two opposite ends of the stirring shaft 107 is connected to the driving part 109 to drive the stirring shaft 107 to rotate by the driving part 109, so as to drive the stirring blades 108 to stir the material. The drive member may be a motor.

Preferably, the stirring blades 108 on the stirring shaft 107 are configured to convectively stir the oily pollutants, so that high-intensity stirring of the oily pollutants can be realized in the heating process, heat can be more efficiently transferred to the oily pollutants, the treatment time is shortened, the treatment efficiency is improved, and the energy consumption is reduced.

As an example, two stirring blade sets are provided on the stirring shaft 107 at intervals in the horizontal direction, and the two stirring blade sets are provided on both sides of the heavy phase outlet 104. Each stirring blade group includes a plurality of stirring blades 108 arranged in a spiral shape, each stirring blade 108 is connected to the stirring shaft 107 by a connecting member (e.g., a connecting rod) and is disposed obliquely with respect to the stirring shaft 107, for example, at an angle of 30 degrees to 50 degrees, and the stirring surface of the stirring blade 108 in each stirring blade group is disposed facing the other stirring blade group.

In the stirring process, the two stirring blade sets respectively push oil-containing pollutants to move from the two ends of the reaction kettle to the area corresponding to the heavy phase outlet 104, the oil-containing pollutants flow from the top of the area corresponding to the heavy phase outlet 104 to the two ends of the reaction kettle, and the oil-containing pollutants are pushed back to the area corresponding to the heavy phase outlet 104 from the two ends by the two stirring blade sets, so that a convection stirring circulation is realized, the high-efficiency treatment of the oil-containing pollutants is realized by continuous convection stirring, and then the heavy components are discharged from the heavy phase outlet 104.

The inclination angle of the stirring blade 108, i.e., the installation angle, refers to an acute angle between the stirring surface of the stirring blade 108 and the axis of the stirring shaft 107. The mixing surface of the mixing blade 108 is the surface that pushes the material into motion during mixing. The stirring blade 108 may be a straight blade, a hinge, a spiral blade, etc., for example, a straight blade, and the stirring surface thereof is a flat surface.

Further, stirring blade 108 has a gap with an inner wall surface of inner housing 105, and the gap has a size of 20mm to 40mm, for example, 25mm to 35mm, and further for example, 30 mm. By providing the above-mentioned space between the stirring blade and the inner wall surface of the inner case 105, the expansion requirement of the case in the heating process can be satisfied to ensure the reliability of the operation of the reaction vessel.

The heating assembly includes a first heating medium chamber 110 and a heating medium in the first heating medium chamber 110. The first heating medium chamber 110 is formed by an outer wall surface of the inner case 105 and an inner wall surface of the outer case 106 spaced from each other. The heating medium is, for example, heat conducting oil, superheated steam, etc., and is fed into the first heating medium cavity 110 to heat the oil-containing pollutants in the first chamber 101.

Further, the heating assembly may further optionally include a plurality of spacers 111 disposed at intervals in the horizontal direction in the first heating medium chamber 110, and the plurality of spacers 111 may divide the first heating medium chamber 110 into a plurality of chamber units independent of each other, each chamber unit including an inlet and an outlet of the heating medium. Through divide into during the stranded a plurality of cavity units of sending into respectively with heating medium, make reation kettle wholly be heated more evenly, temperature control is more accurate, has avoided the problem that local overheat and temperature control degree of difficulty are big, has improved the treatment effeciency to energy saving and consumption reduction.

Further, the chamber unit formed between two adjacent spacer rings 111 is an annular chamber.

Further, the spacer ring 111 is a heat insulating ring.

Further, the heating assembly may further optionally include a heat sink disposed within the chamber unit. The heat sink member includes a heat conductive connection portion 112 and a fin portion 113 connected to each other, and the heat conductive connection portion 112 is connected to an outer wall surface of the inner housing 105 and extends toward the outer housing 106. The number of the fin portions 113 is two or more, and the two or more fin portions 113 are provided at intervals from each other in the extending direction of the heat conductive connecting portion 112. The heating area of the reaction kettle can be increased by arranging the heat absorbing part, the heat of a heating medium is better absorbed, the heat conduction speed is accelerated, and the heat is quickly transferred to oil-containing pollutants.

In some embodiments, the system further comprises a first heating furnace 5, and the heating medium outlet of the first heating furnace 5 is connected to the inlet of the first heating medium chamber 110. The first heating furnace 5 heats heat conduction oil or generates superheated steam, the heated heat conduction oil or the generated superheated steam enters the first heating medium cavity 110 to heat the oil-containing pollutants, and then returns to the first heating furnace 5 to heat again, so that the cyclic utilization of the heating medium is realized.

The oily pollutants are wide in source, complex in composition and form, and may contain floating oil and massive impurities such as metal, stone, bricks and the like. In some embodiments, the system further comprises a crushing device 601 and a homogenizing device 602, wherein the inlet of the homogenizing device 602 is connected to the outlet of the crushing device 601, and the outlet of the homogenizing device 602 is respectively connected to the first inlet 102 of the two or more batch type vacuum distillation apparatuses 1.

The crushing device 601 is used for crushing oil-containing pollutants to crush large impurities in the oil-containing pollutants into fragments with the particle size of less than 30mm, so that the treatment efficiency and the oil recovery rate are improved, and the influence of the large impurities on subsequent processes and devices can be prevented. For large impurities which cannot be broken, the large impurities can be removed by screening. The crushing plant 601 is for example a crusher.

The homogenizing device 602 is used for homogenizing and removing floating oil from the oil-containing pollutant after the crushing treatment, so as to improve the treatment efficiency and the oil recovery rate. For example, the oil-containing pollutant after crushing treatment is mixed with water and heated to 50-80 ℃, such as 60-70 ℃, and is stirred for 10-20 min, so that the oil, water and oil sludge in the oil are primarily separated, the obtained oil is transported out, the water is recycled, and the oil sludge is sent to the batch type reduced pressure distillation device 1 for treatment. The pretreatment removes water and floating oil in the oily pollutants, homogenizes the oily pollutants, can improve the treatment efficiency of subsequent devices, and reduces energy consumption.

Further, in the homogenizing and floating oil removing treatment process, the mass ratio of the oil-containing pollutants to the water is 1: 10-1: 20.

Furthermore, a demulsifier and a flocculant can be added into the mixture of the oil-containing pollutant and the water, so that the separation of oil, water and oil sludge is better promoted.

Further, the system may further comprise a second storage device 7, wherein the second storage device 7 is connected between the homogenizing device 602 and the batch type reduced pressure distillation apparatus 1, and is used for buffering the oil-containing pollutants from the homogenizing device. As an example, the outlet of the homogenizing device 602 may be connected to the inlet of the second storing device 7 by a feeder 8, the feeder 8 being, for example, a lifting conveyor; the discharge hole of the second storage device 7 can be connected with the first feed hole 102 of the batch type reduced pressure distillation device 1 through the first screw conveying device 9, and the oily pollutants are conveyed into the batch type reduced pressure distillation device 1 through the first screw conveying device 9.

Optionally, the first screw conveyer 9 is a forward and backward screw conveyer, which has a feeding port and two discharging ports located at two axially opposite ends of the first screw conveyer, the feeding port is connected to the discharging port of the homogenizing apparatus 602, and the two discharging ports are respectively connected to the first feeding ports 102 of the two batch-type vacuum distillation apparatuses 1, so as to respectively convey the oily pollutants to the two batch-type vacuum distillation apparatuses 1 through the first screw conveyer 9.

In some embodiments, the system further comprises an extractant adding device 10, and the extractant adding device 10 is connected to the upstream of the two or more batch type reduced pressure distillation devices 1 and is used for adding the extractant into the oil-containing pollutants. In the batch type vacuum distillation device 1, under the stirring of the stirring component 104, the extractant is fully contacted with the oily pollutant to extract the light oil in the oily pollutant, so that the operation temperature of the batch type vacuum distillation device 1 can be reduced, the treatment time is shortened, the energy consumption is reduced, and the treatment efficiency is improved.

As the above-mentioned extractant, there are exemplified organic ethers such as methyl t-butyl ether and the like, but not limited thereto. By adopting the extractant, the light components in the oil-containing pollutants can be fully extracted in the vacuum distillation process of the intermittent vacuum distillation device 1, and then the light oil components in the oil-containing pollutants are carried out by utilizing the advantage of low boiling point temperature of the extractant, and are recovered after condensation liquefaction. Due to the solubility and the low boiling point of the extracting agent, the operation temperature of the intermittent reduced pressure distillation device 1 is reduced, the treatment energy consumption is saved, and the treatment efficiency of the intermittent reduced pressure distillation device 1 is improved.

Further, when the system comprises the second storage device 7, an extracting agent inlet may be formed in the second storage device 7, and an extracting agent outlet of the extracting agent adding device 10 is connected to the extracting agent inlet of the second storage device 7. Add the extractant into second storage device 7 in with oily pollutant preliminary mixing to carry oily pollutant to intermittent type formula vacuum distillation device 1's in-process at first screw conveyor 9, make extractant and oily pollutant intensive mixing, can give play to the effect of extractant tentatively, extract out partial light oil in the oily pollutant, be favorable to improving intermittent type formula vacuum distillation device 1's treatment effeciency.

In some embodiments, the system further comprises a first gas extraction device 11, the first gas extraction device 11 is connected with the gas phase outlet 103 of the batch vacuum distillation apparatus 1, and is used for extracting the gas in the first chamber 101 and controlling the reduced pressure environment in the first chamber 101.

Further, the first air extracting device 11 comprises a first condenser 11a and a first vacuum pump 11b, an inlet of the first condenser 11a is connected with the gas phase outlet 103, and a gas outlet of the first condenser 11a is connected with the first vacuum pump 11 b.

In the vacuum distillation process of the batch vacuum distillation apparatus 1, the gas generated by vacuum distillation of the oil-containing contaminants is pumped out by the first vacuum pump 11b so that the inside of the apparatus maintains a high degree of vacuum, and the gas pumped out by the first vacuum pump 11b is condensed and liquefied in the first condenser 11 a. The liquid phase outlets of the first condenser 11a are connected to the recovery water tank 12 and the recovery oil tank 13, respectively, and classified recovery is performed. Wherein, the outlet of the recovery water tank 12 is connected with a water pump 12a to carry out resource outward transportation and recovery on the recovered water; the outlet of the recovered oil tank 13 is connected to an oil pump 13a to carry out the resource outward recovery of the recovered oil.

In the system of the embodiment of the present invention, there may be one first air extractor 11, and the first air extractor 11 is connected to more than two intermittent vacuum distillation apparatuses 1; it is also possible to have two or more first gas extraction devices 11, each first gas extraction device 11 being connected to one or more batch type reduced pressure distillation apparatuses 1, and for example, two or more first gas extraction devices 11 being connected to two or more batch type reduced pressure distillation apparatuses 1 in one-to-one correspondence.

Further, when the system comprises the above-mentioned extractant adding device 10, the system further comprises an extractant recovery tank 14, an inlet of the extractant recovery tank 14 is connected with an extractant outlet of the first condenser 11a, and an outlet of the extractant recovery tank 14 is connected with an inlet of the extractant adding device 10 through an extractant recycling pump 14a, so that the extractant is recycled, and resources are saved.

Further, switching valves 12b, 13b, and 14b are provided on the pipelines between the recovery water tank 12, the recovery oil tank 13, and the extractant recovery tank 14, and the first condenser 11a, respectively, and the classification recovery of water, light oil, and extractant is controlled by the switching valves 12b, 13b, and 14 b.

In some embodiments, the gas phase outlet 103 of the batch vacuum distillation apparatus 1 is provided with a first filter 114, and the first filter 114 is used for filtering the discharged gas, removing particulate matters carried in the gas, improving the quality of the light oil, and avoiding the influence of the particulate matters on subsequent processes and apparatuses. At this time, the first gas evacuation device 11 is connected to the gas phase outlet 103 through the first filter 114.

In some embodiments, the continuous pyrolysis apparatus 2 is used for pyrolyzing heavy components under inert gas or nitrogen protection and micro-positive pressure conditions to obtain pyrolysis gas and residues, the pyrolysis gas includes cracked gas, gasoline gas, diesel gas, lubricating oil gas and the like, and the pyrolysis oil component in the pyrolysis gas is condensed and liquefied and then is classified and recovered. Because the continuous pyrolysis device 2 is used for carrying out pyrolysis treatment on the heavy components under the conditions of inert gas or nitrogen protection and micro-positive pressure, the treatment process has higher safety.

In this context, a slight positive pressure means an absolute pressure of 50Pa to 10kPa above atmospheric pressure, for example an absolute pressure of 50Pa to 5kPa above atmospheric pressure, and further for example an absolute pressure of 50Pa to 500Pa above atmospheric pressure.

In some embodiments, the second chamber 201 of the continuous pyrolysis apparatus 2 sequentially includes a heavy oil pyrolysis section, a semicoke carbonization section, and a mineral decomposition section from the second feeding port 202 side to the residue outlet 204 side, the continuous pyrolysis apparatus 2 further includes a second heating assembly, the second heating assembly is disposed around the second chamber 201, the second heating assembly sequentially includes a plurality of heating zones corresponding to the heavy oil pyrolysis section, the semicoke carbonization section, and the mineral decomposition section, and heating capacities of the plurality of heating zones are sequentially increased from the heavy oil pyrolysis section to the mineral decomposition section.

In these embodiments, the heavy component is fed into the second chamber 201 through the second feeding port 202, and gradually moves from the second feeding port 202 side to the residue outlet 204 side, and sequentially passes through the heavy oil pyrolysis section, the semicoke carbonization section, and the mineral decomposition section during the movement, the heavy component is subjected to heavy oil pyrolysis treatment in the heavy oil pyrolysis section to obtain a first pyrolysis oil component and a first solid phase, the first solid phase is subsequently subjected to semicoke carbonization treatment in the semicoke carbonization section to obtain a second pyrolysis oil component and a second solid phase, and the second solid phase is subsequently subjected to mineral decomposition treatment in the mineral decomposition section to obtain pyrolysis gas and residue. From this, realize the deep treatment of oily solid useless at continuous type pyrolysis device 2, fully retrieved the oil content in the heavy component, effectively reduced the total hydrocarbon content in the residue to salt content in the residue has effectively been reduced, thereby improve the oil content recovery rate in the oily pollutant, make the residue show to reduce ecological environment and human health's harm, satisfy discharge standard, reduce the degree of difficulty of residue processing.

For example, in the heavy oil pyrolysis treatment, under the conditions of inert gas or nitrogen protection and micro-positive pressure, the heavy component is gradually heated from 370 ℃ to 400 ℃ to 450 ℃ to 500 ℃ at a preset heating rate for pyrolysis treatment, so that the heavy oil component in the heavy component is pyrolyzed to obtain a first pyrolysis oil component, and the residual solid waste is a first solid phase.

The semi-coke carbonization treatment is, for example, to gradually increase the temperature of the first solid phase obtained in the heavy oil pyrolysis treatment step from 450 to 500 ℃ to 570 to 600 ℃ at a preset temperature increase rate under the conditions of inert gas or nitrogen protection and micro positive pressure to perform pyrolysis treatment, so that the organic substances in the first solid phase are further pyrolyzed to obtain a second pyrolysis oil component, and the residual solid waste is the second solid phase.

The mineral decomposition treatment is, for example, to gradually raise the temperature of the second solid phase from 570-600 ℃ to more than 600 ℃, for example, 700-1000 ℃, for example, 800-900 ℃, for example, 850 ℃ at a preset temperature raising rate under the conditions of inert gas or nitrogen protection and micro positive pressure, to pyrolyze salt substances in the second solid phase to obtain pyrolysis gas, and the residual solid waste is residue.

The proper treatment temperature of the heavy oil pyrolysis section, the semicoke carbonization section and the mineral substance decomposition section can be determined according to the difference of the compositions of oil-containing pollutants from different sources. As an example, the temperature in the second chamber 201 is gradually increased from 370 ℃ at the side of the second feeding port 202 to more than 600 ℃ at the side of the residue outlet 204, wherein the part in the temperature range of 370 ℃ to 500 ℃ is the heavy oil pyrolysis section, the part in the temperature range of 500 ℃ to 600 ℃ is the semi-coke carbonization section, and the part in the temperature range of more than 600 ℃ is the mineral decomposition section.

Optionally, the continuous pyrolysis apparatus 2 is a rotary kiln type pyrolysis furnace, the rotary kiln type pyrolysis furnace 2 includes an inner furnace body 205 and an outer furnace body 206 that are sleeved with each other, an inner wall surface of the inner furnace body 205 encloses to form a second chamber 201, and an outer wall surface of the inner furnace body 205 and an inner wall surface of the outer furnace body 206 are spaced from each other to form a second heating medium chamber 207; the opposite ends of the inner furnace 205 are rotatably disposed on the outer furnace 206, and the inner furnace 205 is disposed at a predetermined inclined angle with respect to the horizontal direction, so that the second feeding hole 202 side of the second chamber 201 is higher than the residue outlet 204 side.

Heating of the heavy components in the second chamber 201 is achieved by introducing a heating medium, such as hot air, into the second heating medium chamber 207. That is, in this embodiment, the second heating element includes the second heating medium chamber 207 and the heating medium in the second heating medium chamber 207. Optionally, the second heating medium cavity 207 has a medium inlet close to the residue outlet 204 side and a medium outlet close to the second feeding port 202 side, the heating medium is fed into the second heating medium cavity 207 from the residue outlet 204 side, and in the process that the heating medium flows toward the second feeding port 202 side, heat is gradually transferred to the material in the second chamber 201, and as the heating medium continuously flows, the temperature of the material is continuously reduced, so as to meet the heating requirements of different sections in the second chamber 201.

The materials can be fully stirred through the rotation of the inner furnace body 205, so that the materials are uniformly heated, the treatment efficiency is improved, and the energy is saved and the consumption is reduced. Because the second feeding hole 202 side of the second chamber 201 is higher than the residue outlet 204 side, in the rotation process of the inner furnace body 205, the material is conveyed to the residue outlet 204 side from the second feeding hole 202 side, so that a special material conveying assembly is omitted, and the system structure is simplified.

Further, the preset inclination angle of the inner furnace body 205 relative to the horizontal direction is 3-5 degrees, so that the heavy component can be ensured to have enough residence time in the second chamber 201, the oil recovery efficiency can be improved, the total hydrocarbon content in the residue can be effectively reduced, and the salt content in the residue can be effectively reduced.

A rotary kiln type thermal decomposition furnace is adopted, the inner furnace body 205 rotates at a low speed, and the furnace is protected by inert gas or nitrogen and runs at a micro positive pressure, so that higher running safety is ensured.

In some embodiments, the system further comprises a second heating furnace 15, and the hot air outlet of the second heating furnace 15 is connected with the medium inlet of the second heating medium cavity 207. The second heating furnace 15 heats the air to a preset temperature to generate hot air, and the hot air enters the second heating medium cavity 207 to heat the material in the second chamber 201. For example, the second heating furnace 15 provides hot air at 1000 ℃ to meet the heating requirements of a heavy oil pyrolysis section (370-500 ℃), a semicoke carbonization section (500-600 ℃) and a mineral decomposition section (>600 ℃), and the content of Total Petroleum Hydrocarbons (TPH) after treatment is effectively ensured to be less than 0.3 wt%.

The system also optionally comprises a waste heat recovery heat exchanger 16, wherein a heat source side inlet of the waste heat recovery heat exchanger 16 is connected with a medium outlet of the second heating medium cavity 207, a heat source side outlet of the waste heat recovery heat exchanger 16 is connected with a chimney 17, a cold source side inlet of the waste heat recovery heat exchanger 16 is communicated with the atmosphere, and a cold source side outlet of the waste heat recovery heat exchanger 16 is connected with a combustion-supporting gas inlet of the second heating furnace 15. Wherein, the heat source side outlet of the waste heat recovery heat exchanger 16 can be connected with a chimney 17 through an induced draft fan 18, and the cold source side inlet can be communicated with the atmosphere through a combustion fan 19.

The hot air heated by the continuous pyrolysis device 2 is introduced into the waste heat recovery heat exchanger 16 through the induced draft fan 18, and exchanges heat with the air introduced by the combustion fan 19 to form high-temperature combustion-supporting air, so that waste heat recovery is realized, and the waste heat recovery utilization rate is improved. The air is preheated and then introduced into the second heating furnace 15, so that the energy-saving effect of the second heating furnace 15 is achieved, the fuel consumption of the second heating furnace 15 is reduced, and the heating energy consumption is saved. The low-temperature hot air after heat exchange is sent into a chimney 17 by a draught fan 18 to be discharged.

Further, the system also comprises a catalyst adding device 20, and the catalyst adding device 20 is connected between the intermittent reduced pressure distillation device 1 and the continuous pyrolysis device 2 and is used for adding a catalyst into the heavy components. Under the catalytic action of the catalyst, the operation temperature of the continuous pyrolysis device 2 is favorably reduced, the reaction speed is increased, the treatment efficiency is improved, the energy consumption is reduced, the recovery rate of pyrolysis oil content can be increased, and particularly the recovery rate of gasoline oil content and diesel oil content is increased. The catalyst is, for example, a micro-bead molecular sieve catalyst, but is not limited thereto.

Optionally, when the system includes the first storage device 4, the first storage device 4 has a catalyst inlet, and the catalyst outlet of the catalyst adding device 20 is connected to the catalyst inlet of the first storage device 4, so as to add the catalyst into the heavy components buffered in the first storage device 4.

Further, the discharge port of the first storage device 4 is connected with the second feed port 202 of the continuous pyrolysis device 2 through the second screw conveyor 21. The heavy component is fed into the continuous pyrolysis apparatus 2 by the second screw conveyor 21, and the material containing the heavy component and the catalyst is stirred during the conveyance process, so that the catalyst is dispersed in the heavy component, and the above effects can be exhibited more effectively.

In some embodiments, the system further comprises a second gas extraction device 22, the second gas extraction device 22 being connected to the pyrolysis gas outlet 203 of the continuous pyrolysis device 2 for extracting the pyrolysis gas from the second chamber 201.

Further, the second air extractor 22 comprises a second condenser 22a and a second vacuum pump 22b, an inlet of the second condenser 22a is connected with the pyrolysis gas outlet 203, and a gas outlet of the second condenser 22a is connected with the second vacuum pump 22 b.

In the pyrolysis process of the continuous pyrolysis apparatus 2, the pyrolysis gas in the continuous pyrolysis apparatus 2 is pumped out by the second vacuum pump 22b, and the pumped pyrolysis gas enters the second condenser 22a to be condensed and liquefied. The liquid phase outlet of the second condenser 22a is connected to a recovery oil tank 23 to perform classified recovery of pyrolysis oil components. Wherein, the outlet of the oil recovery tank 23 is connected with an oil pump 23a to carry out resource outward transportation and recovery on the recovered oil.

In some embodiments, the pyrolysis gas outlet 203 of the continuous pyrolysis apparatus 2 is provided with the second filter 24, which is used for filtering the pyrolysis gas, removing particles carried in the pyrolysis gas, improving the quality of pyrolysis oil, and avoiding the influence of the particles on the subsequent processes and apparatuses. For example, the second filter 24 is a cyclone filter, which has high separation efficiency. At this time, the second gas-withdrawal device 22 is connected to the pyrolysis gas outlet 203 via the second filter 24.

The first air extractor 11 and the second air extractor 22 can generate noncondensable gas which cannot be condensed, the noncondensable gas mainly comprises C4-containing components, such as butane, ethane, ethylene, methane, hydrogen, carbon monoxide and the like, direct emission can cause environmental pollution and influence human health, the noncondensable gas has higher calorific value, the noncondensable gas can be used as fuel to fully utilize the calorific value, energy is saved, and harmless standard emission of waste gas is realized.

In some embodiments, further include noncondensable gas processing apparatus 25, the gas inlet of noncondensable gas processing apparatus 25 is connected respectively in the noncondensable gas export of foretell first vacuum pump 11b and the noncondensable gas export of second vacuum pump 22b, send noncondensable gas into noncondensable gas processing apparatus 25, carry out purification treatment to noncondensable gas through noncondensable gas processing apparatus 25, for example desulfurization treatment or SOx/NOx control treatment, can avoid the noncondensable gas to contain harmful substance such as sulphide (for example sulfur dioxide, sulfur trioxide, hydrogen sulphide etc.) in the hot-blast that obtains as fuel, satisfy emission standard.

The noncondensable gas treatment device 25 may employ a wet desulfurization (desulfurization/denitrification) device such as a spray tower. The spray tower comprises a gas distributor, a packing layer, a spray assembly and a demister from bottom to top in sequence. The noncondensable gas gets into the spray column by the tower bottom in, with the washing liquid countercurrent contact who sprays by spray assembly to absorb sulphide (sulphide and nitride) in the noncondensable gas with the washing liquid, can make noncondensable gas and washing liquid contact more fully through setting up the packing layer, improve purification efficiency. Demisting the purified noncondensable gas by a demister, and then sending the demisted gas to be used as fuel for combustion and utilization. For example, the fuel is sent to the first heating furnace 5 and/or the second heating furnace 15 for resource utilization as auxiliary fuel.

As a specific example, the gas outlet of the noncondensable gas treatment device 25 is connected to the combustion-supporting gas inlet of the second heating furnace 15, and the noncondensable gas purified by the noncondensable gas treatment device 25 is sent to the second heating furnace 15 to be used as auxiliary fuel for resource utilization.

The above-mentioned washing liquid can adopt the known washing liquid that is used for desulfurization (SOx/NOx control), the utility model discloses do not do the concrete restriction. As an example, the desulfurization scrubbing solution can be a caustic, such as NaOH caustic, or the like.

The residue outlet 204 of the continuous pyrolysis device 2 may be connected to the discharging machine 26, and the residue after pyrolysis treatment of the heavy components is discharged to the outside through the discharging machine 26. The outfeed machine 26 is, for example, a lifting conveyor.

The first condenser 11a and the second condenser 22b are not particularly limited, and condensers that can condense the light oil fraction, the extractant, the cracked oil fraction, and the like, such as a direct cooling heat exchanger, may be selected according to actual needs.

The cooling systems for the first condenser 11a and the second condenser 22b may be selected according to actual requirements. As an example, the coolant inlet of the first condenser 11a is connected to the coolant outlet of the coolant buffer tank 272 via a coolant circulation pump 271, the coolant outlet of the first condenser 11a is connected to the coolant inlet of the air cooler 273, and the coolant outlet of the air cooler 273 is connected to the coolant inlet of the coolant buffer tank 272, thereby forming a circulation circuit of the coolant. And condensing and liquefying the high-temperature gas by adopting a cooling liquid circulating cooling mode. When two or more first condensers 11a are provided, one cooling system may be used in common. The cooling system of the second condenser 22a can refer to the cooling system of the first condenser 11a, and will not be described in detail herein.

In order to improve the treatment effect of the batch type vacuum distillation apparatus 1 and the continuous pyrolysis apparatus 2, the inner shell 105 and the inner furnace 205 are made of a material having a good heat conductivity, and the outer shell 106 and the outer furnace 206 are made of a material having a good heat insulating property.

In some embodiments, the system may further include a central DCS intelligent control system, which is disposed in the central control room and is used to uniformly regulate and control the whole process, and adjust process parameters such as rotation speed, temperature, pressure, flow rate, etc. in real time according to actual conditions, so as to implement automatic control and management.

Adopt the utility model provides an oily pollutant preface batch continuous processing system, higher suitability has to various oily pollutants, innocent treatment and resource recycle to the oily pollutant of various sources have been realized well, higher oil content rate of recovery has, be more than 95%, total petroleum hydrocarbon content is below 0.3 wt% in the residue that obtains, main pollutant emission index satisfies "oil refining industry pollutant discharge standard" (GB31570-2015), satisfy strict environmental protection requirement, and can contain the bacterium in the oily pollutant of exterminating, higher treatment effeciency has simultaneously, the processing procedure stability and security are higher, can also the energy saving, reduce the energy consumption.

The utility model provides a continuous processing system is criticized to oily pollutant preface owing to still adopted noncondensable gas burn back, hot-blast waste heat recovery etc. has improved energy utilization and has rateed, and waste heat recovery rate is more than 90%, practices thrift the energy consumption more than 50%.

The utility model provides a continuous type processing system is criticized to oily pollutant preface extensively is applicable to the green of various oily pollutants such as oil field, petroleum and chemical industry, accident fatlute and handles.

Next, a sequential batch continuous treatment method for oil-containing pollutants according to an embodiment of the present invention will be described with reference to fig. 2 and 3. Referring to fig. 2, a sequential batch continuous processing method of oil-containing pollutants according to an embodiment of the present invention includes a sequential batch vacuum distillation processing step S100 and a continuous pyrolysis processing step S200.

S100, dividing the oil-containing pollutant to be processed into more than two batches, and respectively sending the batches into more than two intermittent reduced pressure distillation devices for processing, wherein each intermittent reduced pressure distillation device carries out intermittent reduced pressure distillation processing on the oil-containing pollutant to obtain light oil and heavy components, and the more than two intermittent reduced pressure distillation devices send the heavy components out in batches according to a preset sequence.

And S200, continuously feeding the heavy components into a continuous pyrolysis device for pyrolysis treatment to obtain pyrolysis oil and residues.

According to the utility model discloses oily pollutant preface batch continuous type processing method, divide into the oily pollutant of pending two above batches and send into two above intermittent type formula vacuum distillation plant respectively, every intermittent type formula vacuum distillation plant carries out intermittent type formula vacuum distillation to oily pollutant and handles and obtain light oil content and heavy component. Because of the adoption of the intermittent reduced pressure distillation operation, the device has no special requirements on the shape, the composition, the water content, the shape of the contained impurities, the impurity rate, the oil content and the like of the oily pollutants to be treated, has higher adaptability to the oily pollutants and can treat the oily pollutants from various sources.

Because of the adoption of the intermittent reduced pressure distillation operation, the intermittent reduced pressure distillation device has good tightness in the operation process, greatly reduces the distillation operation temperature, has balanced internal pressure and convenient control, prevents air leakage, and ensures lower oxygen content and higher vacuum degree in the device, thereby ensuring that the intermittent reduced pressure distillation device has higher stability and safety in the operation process, improving the recovery efficiency of light oil content, saving energy and reducing consumption.

The two or more intermittent reduced pressure distillation devices send out heavy components in batches according to a preset sequence, so that the heavy components are continuously provided for the continuous pyrolysis device, the continuous pyrolysis device continuously receives the heavy components, and the heavy components are pyrolyzed to obtain pyrolysis oil and residues, so that the treatment method has higher treatment efficiency and is suitable for treating large-batch oil-containing pollutants.

Because the water in the oily pollutant is removed in the intermittent reduced pressure distillation device and a large amount of oil in the oily pollutant is recovered, the oil content in the obtained heavy component is obviously reduced, the disturbance of the water to the treatment process is avoided in the treatment process of the continuous pyrolysis device, the process stability is higher, the oil recovery rate in the oily pollutant is improved, the treatment efficiency is further improved, and the energy consumption of the continuous pyrolysis device is obviously reduced.

Referring to fig. 3, in some embodiments, the sequencing batch vacuum distillation processing step S100 may include a dehydration step S110 and a light oil recovery step S120.

S110, heating the oil-containing pollutants from the normal temperature to 50 ℃ to 150-180 ℃ according to a preset heating rate at an absolute pressure of below 50kPa, and carrying out reduced pressure distillation and dehydration.

And S120, gradually heating the dehydrated oil-containing pollutants to 370-400 ℃ from 150-180 ℃ according to a preset heating rate at an absolute pressure of below 50kPa, and carrying out reduced pressure distillation treatment to obtain the light oil and heavy components.

In some embodiments, in the continuous pyrolysis step S200, the heavy components are pyrolyzed under inert gas or nitrogen protection and micro-positive pressure conditions to obtain pyrolysis gas and residues, where the pyrolysis gas includes cracked gas, gasoline gas, diesel gas, lubricating oil gas, and the like, and the pyrolysis oil is condensed and liquefied and then is recycled in a classified manner. Because the continuous pyrolysis device carries out pyrolysis treatment on the heavy components under the conditions of inert gas or nitrogen protection and micro-positive pressure, the treatment process has higher safety.

Further, the continuous pyrolysis treatment step S200 may include a heavy oil pyrolysis step S210, a semi-coke carbonization step S220, and a mineral decomposition step S230.

S210, under the conditions of inert gas or nitrogen protection and micro-positive pressure, the heavy component is gradually heated from 370-400 ℃ to 450-500 ℃ according to a preset heating rate for pyrolysis treatment, and a first pyrolysis oil component and a first solid phase are obtained.

And S220, under the conditions of inert gas or nitrogen protection and micro-positive pressure, gradually heating the first solid phase from 450-500 ℃ to 570-600 ℃ according to a preset heating rate, and carrying out pyrolysis treatment to obtain a second pyrolysis oil component and a second solid phase.

And S230, under the conditions of inert gas or nitrogen protection and micro-positive pressure, gradually heating the second solid phase from 570-600 ℃ to more than 600 ℃ according to a preset heating rate, and carrying out pyrolysis treatment to obtain pyrolysis gas and residues.

In some embodiments, the method further comprises a preprocessing step S300, and further, the preprocessing step S300 comprises a crushing step S310 and a homogenizing step S320.

S310, crushing the oil-containing pollutants to crush large impurities in the oil-containing pollutants into fragments with the particle size of less than 30 mm. For large impurities which cannot be broken, the large impurities can be removed by screening.

And S320, homogenizing and removing floating oil from the oil-containing pollutants after crushing treatment so as to improve the treatment efficiency and the oil content recovery rate.

For example, in step S320, the oil-containing pollutant after the crushing treatment is mixed with water and heated to 50 to 80 ℃, for example, 60 to 70 ℃, and stirred for 10 to 20min, so that oil, water and oil sludge in the oil are primarily separated, the obtained oil is transported out, the water is recycled, and the oil sludge is sent to a batch vacuum distillation device for treatment.

Further, in step S320, the mass ratio of the oil-containing pollutants to the water is 1: 10-1: 20.

Further, in step S320, a demulsifier and a flocculant may be further added to the mixture of the oil-containing pollutant and the water, so as to better promote the separation of the oil, the water and the oil sludge.

In some embodiments, an extractant may also be added to the oil-containing contaminant prior to step S100. For example, after step S300 and before step S100, an extractant is added to the oil-containing contaminant.

As the above-mentioned extractant, there are exemplified organic ethers such as methyl t-butyl ether and the like, but not limited thereto.

In some embodiments, prior to step S200, a catalyst may also be added to the heavy components. Optionally, after step S100 and before step S200, a catalyst is added to the heavy components.

The catalyst is, for example, a micro-bead molecular sieve catalyst, but is not limited thereto.

The aforesaid is according to the utility model discloses oily pollutant preface batch continuous processing system's technical feature also can be applied to according to the utility model discloses in an oily pollutant preface batch continuous processing method of embodiment, the utility model discloses an oily pollutant preface batch continuous processing method consequently also has corresponding technological effect, no longer gives redundant details here.

Adopt the utility model provides an oily pollutant preface batch continuous processing method, higher suitability has to various oily pollutants, innocent treatment and resource recycle to the oily pollutant of various sources have been realized well, higher oil content rate of recovery has, be more than 95%, total petroleum hydrocarbon content is below 0.3 wt% in the residue that obtains, main pollutant emission index satisfies "oil refining industry pollutant discharge standard" (GB31570-2015), satisfy strict environmental protection requirement, and can contain the bacterium in the oily pollutant of exterminating, higher treatment effeciency has simultaneously, the processing procedure stability and security are higher, can also the energy saving, reduce the energy consumption.

The utility model provides a continuous processing method is criticized to oily pollutant preface owing to still adopted noncondensable gas burn-back, hot-blast waste heat recovery etc. has improved energy utilization, and waste heat recovery utilization is more than 90%, practices thrift the energy consumption more than 50%.

The utility model provides a continuous processing method is criticized to oily pollutant preface, the green who extensively is applicable to various oily pollutants such as oil field, petroleum and petrochemical industry, accident sludge handles.

While the invention has been described with reference to specific embodiments, it will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.

Claims (21)

1. A continuous batch treatment system for oily pollutants, comprising:

the device comprises more than two intermittent reduced pressure distillation devices, wherein each intermittent reduced pressure distillation device comprises a first chamber, and a first feed inlet, a gas phase outlet and a heavy phase outlet which are communicated with the first chamber, valves are respectively arranged on the first feed inlet and the heavy phase outlet, and the more than two intermittent reduced pressure distillation devices discharge heavy components in batches according to a preset sequence;

continuous type pyrolysis device, continuous type pyrolysis device include the second cavity and with second feed inlet, pyrolysis gas export and the residue export of second cavity intercommunication, the second feed inlet respectively with more than two intermittent type formula vacuum distillation device heavy phase exit linkage, continuous type pyrolysis device receives in succession the heavy component is handled and is obtained pyrolysis oil content and residue.

2. The system according to claim 1, further comprising a first storage device for buffering the heavy components, wherein an inlet of the first storage device is respectively connected with heavy phase outlets of more than two batch vacuum distillation devices, and an outlet of the first storage device is connected with the second feeding hole of the continuous pyrolysis device.

3. The system of claim 2, further comprising a catalyst adding device connected between the batch vacuum distillation device and the continuous pyrolysis device, and used for adding a catalyst into the heavy components.

4. The system of claim 3, wherein the first storage device has a catalyst inlet, and the catalyst outlet of the catalyst dosing device is connected to the catalyst inlet.

5. The system of claim 1, wherein the batch vacuum distillation apparatus further comprises:

the stirring assembly is arranged in the first cavity and is used for stirring the oil-containing pollutants;

a first heating assembly disposed around the first chamber for heating the oil-containing contaminant.

6. The system of claim 5, wherein the batch vacuum distillation apparatus comprises an inner shell and an outer shell, the inner shell and the outer shell are sleeved with each other, the inner wall surface of the inner shell encloses to form the first chamber, and the outer wall surface of the inner shell and the inner wall surface of the outer shell are spaced from each other to form the first heating medium chamber.

7. The system of claim 6, further comprising a first heater, wherein the hot air outlet of the first heater is connected to the inlet of the first heating medium chamber.

8. The system of claim 1, wherein the second chamber comprises a heavy oil pyrolysis section, a semicoke carbonization section and a mineral decomposition section in sequence from the second feeding port side to the residue outlet side;

the continuous type pyrolysis device still includes second heating element, encircles the setting of second cavity, second heating element corresponds heavy oil pyrolysis section, semicoke carbonization section and mineral substance decomposition section include a plurality of heating zones in proper order, and is a plurality of the heating power of heating zone by heavy oil pyrolysis section to mineral substance decomposition section rise in proper order.

9. The system of claim 8, wherein the continuous pyrolysis device is a rotary kiln type pyrolysis furnace, the rotary kiln type pyrolysis furnace comprises an inner furnace body and an outer furnace body which are sleeved with each other, the inner wall surface of the inner furnace body encloses to form the second chamber, and the outer wall surface of the inner furnace body and the inner wall surface of the outer furnace body are spaced from each other to form a second heating medium chamber;

the relative both ends of interior furnace body rotationally set up in outer furnace body, just interior furnace body is preset inclination setting with the horizontal direction, the second cavity the second feed inlet side is higher than the residue outlet side.

10. The system of claim 9, wherein said second heating medium chamber has a medium inlet on a side close to said residue outlet and a medium outlet on a side close to said second feed opening, said system further comprising a second heating furnace, a hot air outlet of said second heating furnace being connected to said medium inlet.

11. The system of claim 10, further comprising a waste heat recovery heat exchanger, wherein a heat source side inlet of the waste heat recovery heat exchanger is connected with the medium outlet, a heat source side outlet of the waste heat recovery heat exchanger is connected with a chimney, a cold source side inlet of the waste heat recovery heat exchanger is communicated with the atmosphere, and a cold source side outlet of the waste heat recovery heat exchanger is connected with the combustion-supporting gas inlet of the second heating furnace.

12. The system of claim 1, further comprising:

the first air extractor is connected with the gas phase outlet and used for extracting gas in the first cavity and controlling the reduced pressure environment in the first cavity;

and the second air extractor is connected with the pyrolysis gas outlet and used for extracting the pyrolysis gas in the second chamber.

13. The system of claim 12, wherein the first gas evacuation device comprises a first condenser and a first vacuum pump, an inlet of the first condenser is connected to the gas phase outlet, and a gas outlet of the first condenser is connected to the first vacuum pump;

the second air extractor comprises a second condenser and a second vacuum pump, an inlet of the second condenser is connected with the pyrolysis gas outlet, and a gas outlet of the second condenser is connected with the second vacuum pump.

14. The system according to claim 13, further comprising a non-condensable gas treatment device for performing purification treatment on non-condensable gas, wherein the non-condensable gas outlet of the first vacuum pump and the non-condensable gas outlet of the second vacuum pump are respectively connected with an inlet of the non-condensable gas treatment device, and the non-condensable gas discharged from an outlet of the non-condensable gas treatment device is used as fuel.

15. The system of claim 12, further comprising a crushing device and a homogenizing device, wherein the inlet of the homogenizing device is connected to the outlet of the crushing device, the outlet of the homogenizing device is respectively connected to the first inlets of the two or more batch vacuum distillation apparatuses, the crushing device is configured to crush the oily pollutants, and the homogenizing device is configured to homogenize and remove the oil slick from the crushed oily pollutants.

16. The system of claim 15, further comprising a second holding device connected between the homogenizing apparatus and the batch vacuum distillation apparatus for buffering oil-containing contaminants from the homogenizing apparatus.

17. The system of claim 16, further comprising an extractant adding device connected to the upstream of more than two batch vacuum distillation devices for adding an extractant to the oil-containing pollutant.

18. The system of claim 17, wherein the second storing device is provided with an extracting agent inlet, and an extracting agent outlet of the extracting agent adding device is connected with the extracting agent inlet.

19. The system of claim 17, further comprising an extractant recovery tank, wherein an inlet of the extractant recovery tank is connected with the extractant outlet of the first air extractor, and an outlet of the extractant recovery tank is connected with an inlet of the extractant dosing device.

20. The system according to claim 1, wherein the gas phase outlet is provided with a first filter for filtering the gas;

and/or the pyrolysis gas outlet is provided with a second filter for filtering the pyrolysis gas.

21. The system of claim 20, wherein the second filter is a cyclone filter.

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