CN209292290U - A kind of oil-sand and greasy filth comprehensive utilization device - Google Patents
A kind of oil-sand and greasy filth comprehensive utilization device Download PDFInfo
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- CN209292290U CN209292290U CN201822098994.1U CN201822098994U CN209292290U CN 209292290 U CN209292290 U CN 209292290U CN 201822098994 U CN201822098994 U CN 201822098994U CN 209292290 U CN209292290 U CN 209292290U
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Abstract
The utility model discloses a kind of oil-sands and greasy filth comprehensive utilization device, specifically, the processing unit (plant) of the utility model includes crushing plant (L), premixing device (T), carbonization reactor (A), pre-reactor (F), settler (B), heater (G), calcinatory (J), heat collector (M), quencher (R), washer (N), liquid-solid separator (P), heavy oil heat exchanger (O), middle section extraction oil heat exchanger (Q) and upper section extraction oil heat exchanger (U), and specific connection is detailed in specification.The processing method carried out using described device is by carrying out clean and effective processing to oil-sand and greasy filth and tailings is innoxious and recycling treatment, it adapts to that wide, good product quality, energy utilization are good, advantages of environment protection with raw material, a high efficiency will be provided for oil-sand and oil-sludge treatment, cleaned, recycling, innoxious processing route.
Description
Technical field
The utility model belongs to oil-sand processing and utilization field, and in particular to a kind of comprehensive utilization device of oil-sand and greasy filth.
Background technique
Oil-sand also known as Tar sands or tar sand are a kind of sand or sandstone containing oil, are a kind of non-conventional oil resource, mesh
The proved reserves that natural oil is alreadyd exceed containing oilreserves of preceding oil-sand, are mainly distributed on Canada, Venezuela, Indonesia, Russia
Ross and China etc. are national.
Oil-sand is made of the core of sand grains and the oil film that is surrounded by, basic composition is silt, clay, oil, water and
Inorganic mineral etc. is usually solid-state under room temperature, and under normal circumstances, solid content about 70%~80% in oil-sand, oil content is usual
It is 10~30%.According to architectural characteristic, oil-sand is divided into hydrophily, lipophilicity and neutral three classes.Hydrophily oil-sand refers to oil and sand
There are moisture films between body, are Canadian Athabasca oil-sand than more typical hydrophily oil-sand；Lipophilic oil-sand is oil and sand
Body directly contacts, and instrument detects the presence less than water in oil-sand；And the characteristic of neutral oil-sand is in hydrophily and lipophilic the two
Between.
The exploitation mode of oil-sand resource usually has according to its buried depth: steaming can be used for burying deeper oil-sand
Vapour is handled up method, steam assisted gravity drainage method (SAGD) method, injection solvent method, underground catalytic reforming production technique and hydro-thermal on the spot
Cracking technique etc., the oil-sand shallower for buried depth use surface mining.The oil-sand separation oil-sand that surface mining obtains
In oil, main following three kinds of modes at present: WATER-WASHING METHOD, solvent extraction and method for destructive distillation.
WATER-WASHING METHOD is to mix smashed oil-sand with hot water, then separated by modes such as stirring, flotation, centrifugation and standings
Oil in oil-sand out, WATER-WASHING METHOD are the first tar sand oil extraction processes for being commercialized application.WATER-WASHING METHOD is simply easy to industrial metaplasia
It produces, but is also faced with serious environmental issue.Washing process extraction tar sand oil water consumption is huge, produces one barrel of oil and about consumes four barrels of water,
A large amount of tailing is generated simultaneously, is mixed dampening, tiny particle, clay and residual bitumen/heavy oil in tailing, is contained cycloalkanes simultaneously
The components such as acid, aromatic hydrocarbon and naphtha, so that tailing problem is difficult to handle, in addition, WATER-WASHING METHOD is preferable to hydrophily oil-sand effect,
And it is poor to lipophilic oil-sand extraction effect.
Solvent extraction be by solvent from oil-sand extraction oil, then be recovered by distillation solvent recycle process,
For solvent extraction for WATER-WASHING METHOD, applicability is wider, and separates more efficient；But solvent extraction easily causes
Waste of solvent and environmental pollution, solvent cost is high, and solvent recovery energy consumption is high, currently, there has been no industrial applications for solvent extraction.
Oil-sand cracking process, which refers to, heats oil-sand in the environment of starvation (or air), makes the fry dried food ingredients in oil-sand
Raw cracking reaction plays the role of decarburization and improves C/Hratio, improves oil property, compare WATER-WASHING METHOD and solvent extraction,
Oil-sand cracking process has the characteristics that raw material adaptation is wide, oil quality is good, environment influence is small, will become the oil-sand produced and be added
The development trend that work utilizes, has a extensive future.
For the oil-sand processing and utilization that produces, corresponding methods and techniques are in development phase at present, in existing method
With extraction oily in oil-sand is mostly paid close attention in technology, and ignore innoxious, the recycling treatment of remaining tailings after oil extract.
Oil-sand manufacture field be badly in need of it is a kind of for the oil-sand that produces carry out clean and effective processing and tailings it is innoxious and
The method for comprehensive processing of recycling treatment.
Oily sludge is the oil-containing solids generated during oil exploitation, transport, storage, refining and oily waste water treatment
Waste.In China's oil chemical industries, 800,000 ton tank bed muds, bottom of pond mud are generated every year on average.In oily sludge containing benzene homologues,
The noxious material of the foul smellings such as phenols, anthracene, pyrene not only pollutes environment if not being pocessed, but also causes the waste of resource.I
State's disposal of oily sludge level is low, and processing method is single, and the harmful substance in oily sludge can cause atmosphere, soil, water body
Petroleum sludge is included in " National Hazard waste catalogue " by environmental pollution, therefore, China.
Oily sludge is complex in composition, and this field temporarily can handle without a kind of processing technique of maturation all types of at present
Oily sludge, therefore, this field need the sump oil that a kind of adaptability to raw material is strong, resource utilization is good, harmless treatment degree is high
Processing technique meets the needs of oil-sludge treatment.
Utility model content
Clean and effective processing is carried out the purpose of this utility model is to provide a kind of pair of oil-sand and greasy filth and tailings is harmless
Change the method and device with recycling treatment.
The technical solution of the utility model is:
Providing a kind of oil-sand and greasy filth comprehensive utilization device, described device includes crushing plant L, premixing device T, destructive distillation
Reactor A, pre-reactor F, settler B, heater G, calcinatory J, heat collector M, quencher R, washer N, liquid-solid separator
P, heavy oil heat exchanger O, middle section extraction oil heat exchanger Q and upper section extract oil heat exchanger U out；
Settler settling section setting up and down and stripping section；Including level-one gas-solid separator C, second level gas-solid separator D
With gas distributor E；The level-one gas-solid separator C and second level gas-solid separator D belongs to settling section, level-one gas-solid separator C
It is arranged inside settler, second level gas-solid separator D is arranged inside or outside settler；The gas distributor E belongs to gas
Section is proposed, the lower part inside settler is set；
The heater includes gas-solid separator H and gas distributor I；The gas-solid separator is arranged in heater body
Or it is external；The lower part of heater body is arranged in the gas distributor；
The calcinatory includes gas distributor K；The lower part inside calcinatory is arranged in the gas distributor K；
Wherein, crushing plant entrance is connected with heat collector outlet, and crushing plant outlet is connected with carbonization reactor entrance；In advance
Mixing device entrance is connected with the outlet of upper section extraction oil heat exchanger, and premixing device outlet is connected with carbonization reactor entrance；Destructive distillation is anti-
Device outlet is answered to be connected with the level-one gas-solid separator inside settler, carbonization reactor entrance exports with crushing plant respectively, is pre-
Mixing device outlet is connected with pre-reactor outlet；Pre-reactor entrance is connected with settler outlet, liquid-solid separator outlet respectively,
Pre-reactor outlet is connected with carbonization reactor entrance；Settler lower part outlet is connected with pre-reactor, calorifier inlets respectively；
Heater lower part outlet is connected with pre-reactor and calcinatory entrance respectively；The distribution of the gas of calcinatory upper outlet and heater
Device is connected, and calcinatory lower part outlet is connected with heat collector entrance；
Second level gas-solid separator in settler is connected with quencher entrance, quencher outlet and washer bottom inlet phase
Even；Washer bottom is equipped with outlet and is connected with liquid-solid separator entrance；Liquid-solid separator outlet respectively with pre-reactor, mink cell focus
Heat exchanger entrance is connected；Mink cell focus heat exchanger exit is connected with washer lower part；Outlet and quencher phase are equipped in the middle part of washer
Even；
Upper section extraction oil heat exchanger entrance and exit is connected in the middle part of washer and top respectively, and upper section extracts oil heat exchanger out
On be additionally provided with outlet and be connected with premixing device；Middle section extract out oil heat exchanger entrance and exit respectively in the middle part of washer up and down
It is connected；And the entrance of middle section extraction oil heat exchanger is arranged in the connecting tube of washer and quencher.
Preferably, settler lower part and heater are equipped with connecting tube, set regulating valve in connecting tube.
Preferably, settler lower part and pre-reactor are equipped with connecting tube, set regulating valve in connecting tube.
Preferably, heater lower part and pre-reactor are equipped with connecting tube, set regulating valve in connecting tube.
Preferably, heater lower part and calcinatory are equipped with connecting tube, set regulating valve in connecting tube.
Preferably, calcinatory lower part and heat collector are equipped with connecting tube, set regulating valve in connecting tube.
Preferably, external source entrance is optionally provided in the carbonization reactor.
Preferably, the crushing plant is equipped with feed(raw material)inlet.
Preferably, the premixing device is equipped with feed(raw material)inlet.
Preferably, the calcinatory, heater and settler are equipped with gas access.
Preferably, the calcinatory is equipped with external fuel inlet and optional exotic high temperature gas access.
Preferably, the heat collector is equipped with output of products mouth.
Preferably, the gas-solid separator is equipped with output of products mouth.
Preferably, the heavy oil heat exchanger, middle section extraction oil heat exchanger and upper section extraction oil heat exchanger are equipped with product
Delivery outlet.
Provide a kind of oil-sand and greasy filth method of comprehensive utilization, including provide above-mentioned oil-sand and greasy filth comprehensive utilization device and
Following steps:
(I) raw material oil-sand and the material from heat collector enter in crushing plant mix and be crushed, and obtain broken oil
Sand charging；
Raw material greasy filth enters in premixing device with the material from upper section extraction oil heat exchanger to be mixed, and is mixed
Greasy filth charging；
Broken oil-sand charging and mixed greasy filth charging respectively enter in carbonization reactor, with the object from pre-reactor
Material carries out dry distillation reactor；The material obtained after dry distillation reactor enters settler and is separated, and isolated gas material enters
Quencher, isolated solid material a part enter heater, and another part returns to pre-reactor；
(II) solid material from settler is heated with the gas from calcinatory in the heater, after heating
Solid material and gas material are obtained after separation to material；Wherein, gas material output is used as product；A part of solid material
It returns in pre-reactor, a part of solid material enters calcinatory and calcined；
The material that solid material from heater obtains after calcining in calcinatory enters heat collector, recovered heat
The material obtained after amount, a part return to crushing plant, and rest part is sent out as product；
(III) gas material from settler enters washer bottom after quencher；
It isolates containing solid mink cell focus washer bottom；Enter liquid-solid separator containing solid mink cell focus to be separated；It isolates
It is low that scrubbing tower is returned after heat exchanger exchanges heat as cleaning solution or output as product containing solid mink cell focus；The Gao Hangu isolated
Mink cell focus, which enters, carries out cracking reaction in pre-reactor；
Washer middle section extraction oil, a part enter quencher as quench oil, and another part extracts oil heat exchange out through middle section
Device returns to scrubbing tower as cleaning solution or output as product after taking heat；
After upper section extraction oil heat exchanger heat exchange, a part enters premix as material and sets washer upper section extraction oil
Standby, another part returns to scrubbing tower as cleaning solution or output and is used as product.
Preferably, the operating condition of carbonization reactor are as follows: pressure is 0.1~0.8MPa, and temperature is 450~600 DEG C.
Preferably, the operating condition of settler are as follows: pressure is 0.1~0.8MPa, and temperature is 450~600 DEG C.
Preferably, the operating condition of pre-reactor are as follows: pressure is 0.1~0.8MPa, and temperature is 480~650 DEG C.
Preferably, the operating condition of crushing plant are as follows: pressure is 0.01~0.5MPa, and temperature is 0~200 DEG C.
Preferably, the operating condition of premixing device are as follows: pressure is 0.01~1.5MPa, and temperature is 20~250 DEG C.
Preferably, the operating condition of heater are as follows: pressure is 0.1~0.8MPa, and temperature is 560~800 DEG C.
Preferably, the operating condition of calcinatory are as follows: pressure is 0.1~1.0MPa, and temperature is 700~1300 DEG C.
Preferably, the operating condition of settler are as follows: pressure is 0.1~4.0MPa, and temperature is 40~1300 DEG C.
Preferably, the operating condition of quencher are as follows: pressure is 0.1~0.8MPa, and temperature is 350~480 DEG C.
Preferably, the operating condition of washer are as follows: pressure is 0.1~0.8MPa, and temperature is 80~400 DEG C.
Preferably, 0.2~8.0 meter per second of carbonization reactor linear gas velocity.
Preferably, 0.2~8.0 meter per second of pre-reactor linear gas velocity.
Preferably, 0.1~3.0 meter per second of settler upper gas linear speed.
Preferably, 0.1~3.0 meter per second of heater upper gas linear speed.
Preferably, 0.1~5.0 meter per second of calcinatory upper gas linear speed.
Preferably, the material obtained after dry distillation reactor enter settler separated comprising steps of
After the material obtained after dry distillation reactor enters settler, separated first by level-one gas-solid separator, through one
The isolated gas material of grade gas-solid separator enters second level gas-solid separator and is separated, and level-one gas-solid separator separates
To solid material enter stripping section；
Enter quencher by the isolated gas material of second level gas-solid separator；It is separated by second level gas-solid separator
Obtained solid returns to settler and enters stripping section；
The solid material a part obtained after stripping section enters heater, and another part returns to pre-reactor.
Preferably, feedstock oil sand grains diameter≤50 centimetre.
Preferably, in the raw material greasy filth, carbon hydrogen element content range: 5~95% (weight).
Preferably, raw material oil-sand passes through broken material particular diameter≤8 millimeter of crushing plant.
Preferably, broken material particular diameter range: 0.03~3 millimeter.
Preferably, the raw material oil-sand can also mix the solid matter of hydrocarbon-containiproducts；The solids of the incorporation
Matter one of is selected from the group or a variety of: lignite, the bituminous coal of adhesive index R.I. < 50, jet coal, anthracite, oil shale, sludge.
Preferably, incorporation partial size≤50 centimetre of the solid matter.
Preferably, mixed ratio≤50% (weight) of the solid matter.
Preferably, the stream material (liquid or containing solid-liquid) of hydrocarbon-containiproducts, institute can be also injected in carbonization reactor
It states stream material and can be fed with broken oil-sand, to carry out destructive distillation together with the charging of the greasy filth of mixing and material from pre-reactor anti-
It answers；The stream material is selected from the group below one or more: heavy oil, residual oil, tar, slurry oil, gutter oil, waste oil, sump oil, shale
Oil.
Preferably, the ratio of the stream material and raw material oil-sand is preferred: 0:100%~50%:50% (weight).
Preferably, the solid content of the stream material is less than 15% (weight).
Preferably, the stream material elemental range: hydrogen content 7~20% (weight), carbon content 75~92% (weight).
Preferably, the ratio of raw material oil-sand and raw material greasy filth are as follows: 100%:0%~100%:95% (weight).
Preferably, oxygen-containing gas is passed through in calcinatory to be calcined in calcinatory with the solid material from heater
Heat supply.
Preferably, external fuel can be filled into the calcinatory to carry out reacting heat supply with oxygen-containing gas.
Preferably, high-temperature gas direct heating can be filled into the calcinatory.
The technical solution of the utility model mainly have it is below the utility model has the advantages that
(1) the utility model solid material oil-sand incorporation destructive distillation tailings mix broken, solves solid material oil-sand
The crushing plant being easy to appear and buffer memory device adhesion blocking, the big blocking of conveyance conduit conveying difficulty and fluidisation due to sticky big
Equipment fluidizes the problems such as difficulty is big；The utility model solid material greasy filth is used as liquid form after mixing with the extraction oil isolated
Into carbonization reactor, solve the problems, such as that solid material greasy filth is difficult to greatly feeding-in solid body due to sticky.
(2) the utility model raw material oil-sand and raw material greasy filth connect in carbonization reactor with the abundant back-mixing of high-temperature heat supply tailings
Touching realizes the rapid cleavage of tar sand oil, since streaming mode can realize quick mass-and heat-transfer, and sets inside carbonization reactor
There is the structure for forcing back-mixing, achieve the effect that abundant back-mixing, so that carbonization reactor interior reaction temperature is uniform, by adjusting high temperature
Heat supply tailings supply can be precisely controlled carbonization reactor interior reaction temperature, it can be achieved that closing in raw material oil-sand and raw material greasy filth
Cracking at suitable temperature is to obtain maximized light oil yield.
(3) on the one hand the pre-reactor that the utility model is arranged before carbonization reactor will be isolated containing solid mink cell focus
Online freshening cracking is carried out, had not only avoided not producing or producing low value less containing solid mink cell focus, but also high value lightweight oil yield can be increased, greatly
Added value of product is improved greatly；On the other hand, high-temperature retorting tailings is carried out before entering carbonization reactor by pre-reactor
Primary pre- cooling, avoids the destructive distillation tailings of excessive temperature from being directly entered carbonization reactor and causes localized hyperthermia and make oil product
Second pyrolysis is more and reduces oil yield；
(4) reaction product of the utility model carbonization reactor passes through level-one gas-solid separator, realizes oil gas and solid tail
The quick separating of sand avoids generation second pyrolysis reaction after dry distillation reactor generates the oily tailings long-time contact with high temperature and drops more
Low oil yield；By the oil gas of level-one gas-solid separator using settler and second level gas-solid separator, to isolate oil gas
Middle major part fine powder solid, greatly reduces the burden of oil gas subsequent wash dedusting.In addition, the stripping section of settler lower part setting
The gas air lift carried secretly in solid is gone out by injection gas, entrainment oil gas is avoided to carry into subsequent heat device and reduce oil gas
Yield.
(5) the characteristics of the utility model heater can be rapidly achieved abundant heat transfer using fluidized bed generates calcinatory
High temperature body containing solid gas heats destructive distillation tailings in the heater, and destructive distillation tailings a part after heating is recycled to reactor heat supply, and one
The tailings product that part can carry out different degrees of high-temperature calcination acquisition high value into calcinatory according to subsequent request (can be used as
The raw materials such as good cement, building materials), to take full advantage of the heat of high temperature body containing solid gas, realize different grade heats
Cascade utilization improves energy utilization efficiency, reduces heat cost and energy consumption.
(6) the utility model is realizing energy cascade by using closed multi-stage heat exchanger mode to high temperature tailings after calcining
While recycling, the problem of can get the destructive distillation tailings product of low temperature, well solved tailings dry colling.
(7) the utility model is mutually tied using high temperature multistage gas solid separation with low temperature multistage washing by containing solid oil gas to destructive distillation
It closes, online dedusting obtains cleaning oil gas, improves added value of product, has well solved oil existing for existing fluidized retoring method
Gas is difficult to the problem of online dedusting.
(8) the utility model carbonization reactor device is while realizing oil-sand dry distillation reactor, can accomplish while recracking
(liquid contains solid-liquid to the flowing material of hydrocarbon-containiproducts, such as heavy oil, residual oil, tar, slurry oil, gutter oil, waste oil, shale
Oil etc.), the solid of the hydrocarbon-containiproducts such as fine coal, oil shale, greasy filth, sludge can also be also mixed, realizes plurality of liquid and solid
The hybrid process of substance.
(9) the utility model carries out clean and effective processing to oil-sand and greasy filth and tailings is innoxious and recycling treatment,
It adapts to that wide, good product quality, energy utilization are good, advantages of environment protection with raw material, will be provided for the processing of oil-sand and greasy filth
One high efficiency cleans, recycling, innoxious processing route.
Detailed description of the invention
Fig. 1 is the schematic diagram of a kind of oil-sand and greasy filth method of comprehensive utilization and device of the utility model.
Specific embodiment
Herein, no more than can be understood as being less than or equal to.
The utility model is further elaborated with reference to the accompanying drawing.Specific embodiment and embodiment are not intended to limit this
The claimed range of utility model.
It is as shown in Figure 1 a kind of oil-sand of the utility model and greasy filth comprehensive utilization device:
The device be equipped with crushing plant L, premixing device T, carbonization reactor A, pre-reactor F, settler B, heater G,
Calcinatory J, heat collector M, quencher R, washer N, liquid-solid separator P and heavy oil heat exchanger O, middle section extraction oil heat exchanger Q,
Upper section extracts oil heat exchanger U out.
Crushing plant entrance is connected with heat collector outlet, and crushing plant outlet is connected with carbonization reactor entrance.It is broken to set
It is standby to be additionally provided with feed(raw material)inlet.Premixing device entrance is connected with the outlet of upper section extraction oil heat exchanger, and premixing device outlet and destructive distillation are anti-
Device entrance is answered to be connected.Feed(raw material)inlet is additionally provided on premixing device.Level-one gas-solid inside carbonization reactor outlet connection settler
Separator C, the entrance (one or more) of carbonization reactor is separately connected pre-reactor outlet, crushing plant exports, premix is set
Standby outlet.Second level gas-solid separator D is set at the top of settler, and second level gas-solid separator may be provided in inside or outside settler；It is heavy
Drop device lower part sets gas distributor E, and settler lower part outlet and pre-reactor are equipped with connecting tube, set regulating valve b in connecting tube；It is heavy
It drops device lower part and heater is equipped with connecting tube, set regulating valve a in connecting tube.Gas-solid separator H, gas-solid point is arranged in heater top
It may be provided in heater body or outside from device；Gas-solid separator is equipped with output of products mouth；Heater lower part sets gas distributor
I.Heater lower part outlet is equipped with the communicating pipe with pre-reactor and calcinatory, is respectively equipped with regulating valve c and d on communicating pipe；It forges
Burner upper entrance is connected with the gas distributor of heater lower part, and calcinatory lower part outlet is connected with heat collector entrance.Take heat
Device is equipped with output of products mouth.Settler second level gas-solid separator is connected with quencher entrance, quencher outlet and washer bottom
Entrance is connected, and washer bottom is equipped with communicating pipe with liquid-solid separator, liquid-solid separator outlet respectively with pre-reactor entrance,
Mink cell focus heat exchanger entrance is connected.Mink cell focus heat exchanger exit is connected with washer lower part and equipped with output of products mouth.Upper section
Extraction oil heat exchanger L entrance and exit is connected with washer middle and upper part and top respectively, and is equipped with output of products mouth.In washer
Portion is connected with quencher；Extraction oil heat exchanger Q entrance and exit in middle section is connected with washer middle part up and down respectively；And the chilling
The connecting tube of device and washer is equipped with the connecting tube with middle section extraction oil heat exchanger Q, for connecting middle section extraction oil heat exchanger Q
Entrance；Middle section extraction oil heat exchanger Q is additionally provided with output of products mouth.
The crushing plant L mixes solid material oil-sand 1-1 with the solid destructive distillation tailings 23 from heat collector
It is broken to form reaction feed 2, solve crushing plant and buffer memory device that solid material oil-sand is easy to appear due to sticky big
The problems such as adhesion blocking, big conveyance conduit conveying difficulty big blocking and fluidizing equipment fluidisation difficulty.Raw material oil-sand 1-1 partial size is little
In 50 centimetres.Broken solid material partial size is not more than 8 millimeters, solid material preferable particle size range after being crushed: 0.03~3 milli
Rice.The solid material oil-sand 1-1 can also mix the solid matter 27 of hydrocarbon-containiproducts, and the solid matter partial size of incorporation is not
Greater than 50 centimetres；It is preferred that lignite, the bituminous coal of adhesive index R.I. < 50, jet coal, anthracite, oil shale, sludge etc.；The ratio of incorporation
Example is not more than 50% (weight).The operating condition of crushing plant L are as follows: pressure is 0.01~0.5MPa, and temperature is 0~200 DEG C.
Formation after the premixing device T mixes solid material greasy filth 1-2 with the extraction oil 46 that washer is isolated
Material 47 enters carbonization reactor as liquid form, solves solid material greasy filth due to sticky and is difficult to asking for feeding-in solid body greatly
Topic.The premixing device T has the function of Forced Mixing, is preferably stirred and recycles mixing apparatus.The solid is former
Expect greasy filth 1-2 carbon hydrogen element content range: 5~95% (weight).The operating condition of premixing device T are as follows: pressure be 0.01~
1.5MPa, temperature are 20~250 DEG C.
Solid material oil-sand 1-1 and solid material greasy filth 1-2 ratio are as follows: 100%:0%~100%:95% (weight).
For the carbonization reactor A using fluidisation pattern, the pressure back-mixing structure with shunting, baffling function is arranged in inside,
Can reaction feed 2, material 47, optional external source 28 be rapidly achieved with the high-temperature material 15 from pre-reactor and sufficiently be returned
Mass-and heat-transfer is mixed, so that carbonization reactor interior reaction temperature is more uniform, it can by adjusting high-temperature heat supply tailings supply
To be precisely controlled carbonization reactor interior reaction temperature, it is maximized light to obtain to realize the cracking of tar sand oil at appropriate temperatures
Oil yield.The external source 28 is the stream material (liquid or containing solid-liquid) of hydrocarbon-containiproducts.Stream material element
Range is preferred: hydrogen content 7~20% (weight), carbon content 75~92% (weight).Stream material type is preferred: heavy oil, residual oil,
Tar, slurry oil, gutter oil, waste oil, sump oil, shale oil etc..The solid content of stream material is preferably smaller than 15% (weight).Flowing
The ratio of substance and raw material oil-sand is preferred: 0:100%~50%:50% (weight).The operating condition of carbonization reactor A are as follows: pressure
Power is 0.1~0.8MPa, and temperature is 450~600 DEG C, 0.2~8.0 meter per second of linear gas velocity.
The pre-reactor F by after settler B air lift destructive distillation tailings 12, from the heat supply tailings of heater G
16 and the Gao Hangu mink cell focus 34 from liquid-solid separator P mixed.The shunting of setting band, baffling function inside pre-reactor F
Back-mixing structure, guarantee the abundant back-mixing contact of destructive distillation tailings, heat supply tailings and Gao Hangu mink cell focus, pre-reactor is on the one hand
Online freshening cracking is carried out containing solid mink cell focus by what is isolated, had not only avoided not producing or producing low value less containing solid mink cell focus, but also can increase
The lightweight oil yield for increasing value, greatly improves value-added content of product；On the other hand, by pre-reactor by high-temperature retorting tail
Sand carries out primary pre- cooling before entering carbonization reactor, and excessive temperature heat supply destructive distillation tailings is avoided to be directly entered carbonization reactor
It causes localized hyperthermia and makes tar sand oil generation second pyrolysis more and reduce oil yield.The operating condition of pre-reactor F are as follows: pressure
For 0.1~0.8MPa, temperature is 480~650 DEG C, 0.2~8.0 meter per second of linear gas velocity.
Level-one gas-solid separator C is set inside the settler B, so that into the reaction mass from A of settler B
3 realize the quick separating of oil gas and solid by level-one gas-solid separator C, and the oil gas that can reduce destructive distillation generation to the greatest extent is solid with high temperature
The second pyrolysis of oil product increases and reduces oil yield after body time of contact is long.The preferred inverted L shape separator of level-one gas-solid separator, list
Grade cyclone separator etc..By level-one gas-solid separator isolate containing solid oil gas 4 by settler after 6 enter second level gas-solid point
From the final dusting that device D carries out oil gas, the oil gas 7 being greatly reduced by second level gas-solid separator D solid fines content to urgency
Cooler R is back to settler by the solid fines that second level gas-solid separator D is isolated.Second level gas-solid separator preferably uses
Two stage cyclone separator, 10~40 meter per second of cyclone inlet linear speed, may be disposed inside or outside settler.By one
The solid 5 that grade gas-solid separator is isolated enters settler lower part stripping section, injects air lift by gas distributor E in stripping section
Gas 29 removes entrained oil qi exhaustion in solid 9, and entrainment oil gas is avoided to carry to heater and reduce oil yield.Settler lower part is set
Herringbone baffle or ring baffle or other structures for improving gas-solid counter current contacting are set, air lift effect is improved.Gas stripping gas 29 can be used
One or more of following gas: steam, carbonization gas, dry gas, hydrogen, methane gas, ethane gas, lighter hydrocarbons gas, nitrogen, titanium dioxide
Carbon, flue gas etc., wherein preferred steam or self-produced carbonization gas are as gas stripping gas.Settler B operating condition are as follows: pressure be 0.1~
0.8MPa, temperature are 450~600 DEG C, 0.1~3.0 meter per second of upper gas linear speed.
The top heater G is solid settling section, and lower part is heat exchanging segment, and the solid 9 from settler is through overregulating
The boosted gas 10 of valve a be promoted to 11 in heater with the progress mixed heat transfer of high temperature body containing solid gas 21 from calcinatory J.Heat exchange
Duan Youxuan uses turbulent fluidized bed pattern, and the gas after gas distributor I distribution improves the distribution of heat exchanging segment flow field, to reach
To sufficient heat transfer effect.Gas after heat exchange is isolated by forming 17 after the solid settling section of top into gas-solid separator H
Gas 18 after most of solid fines is sent out, and solid fines are back in the middle part of heater.Gas-solid separator H preferably uses two-stage
Cyclone separator, 10~40 meter per second of cyclone inlet linear speed, may be disposed at heater G interior or outside.Pass through heater
The high-temperature position heat from calcinatory J high temperature body containing solid gas is utilized in G to greatest extent, removes the heat supply of calcinatory high temperature body containing solid gas
It outside, can also be by filling into oxygen-containing gas 30 and the organic principle exothermic heat of reaction heat supply in destructive distillation tailings, the oxygen-containing gas 30
It is preferred that: air, oxygen rich air, oxygen, air and mixture of steam, oxygen and mixture of steam.The operating condition of heater G are as follows:
Pressure is 0.1~0.8MPa, and temperature is 560~800 DEG C, and linear gas velocity is 0.1~3.0 meter per second.
Destructive distillation tailings 20 from heater G enters calcinatory J by regulating valve d control and passes through gas distributor K's
Oxygen-containing gas 25 carries out exothermic heat of reaction.It, can also be by supplementing external fuel in addition to 25 exothermic heat of reaction of destructive distillation tailings and oxygen-containing gas
26-1 enters calcinatory J and oxygen-containing gas 25 carries out exothermic heat of reaction heat supply, or directly supplements the 26-2 heat supply of exotic high temperature gas.Institute
The oxygen-containing gas 25 stated is preferred: air, oxygen rich air, oxygen, air and mixture of steam, oxygen and mixture of steam；Described
External fuel 26-1 is preferred: carbonization gas, raw coke oven gas, dry gas, natural gas, synthesis gas；The exotic high temperature gas 36 is preferred: high
Warm flue gas, high-temperature synthesis gas, high temperature raw coke oven gas.Destructive distillation tailings can carry out different degrees of height according to subsequent request in calcinatory
Temperature calcining is to obtain the tailings product (can be used as the raw materials such as good cement, building materials) of high value.The operating condition of calcinatory J
Are as follows: pressure is 0.1~1.0MPa, and temperature is 700~1300 DEG C, and linear gas velocity is 0.1~5.0 meter per second.
Calcinatory J is after the calcining tailings 22 of regulating valve e control discharge enters heat collector M heat recovery, a part circulation
To crushing plant, remainder is exported as product 24.The heat collector requires that following manner can be used according to product temperature:
Level-one takes heat, level-one to take heat+second level that heat, level-one is taken to take heat+second level that heat+three-level is taken to take heat.Heat collector can be used it is directly cooling or
The indirect type of cooling, cooling medium are optional: water, steam, flue gas, indifferent gas (nitrogen, carbon dioxide), pyrolysis gas, raw coke oven gas, conjunction
It is 30~700 DEG C by its tailings product temperature control range of heat collector at gas etc..The operating condition of heat collector are as follows: pressure is
0.1~4.0MPa, temperature are 40~1300 DEG C.
Promotion the gas 13-1 and 13-2 is preferred: pyrolysis gas, raw coke oven gas, dry gas, natural gas, the promotion gas 10 are excellent
Choosing: air, steam, air and mixture of steam, oxygen and mixture of steam.
High-temperature oil gas 7 after second level gas-solid separator D isolates most of solid is to quencher R by from washer
The quench oil 38 isolated is cooling, and high-temperature oil gas 7 is quenched to certain temperature or less can avoid oil product in oil gas to greatest extent
Cracking coking and blocking equipment and pipeline.The operating condition of quencher R are as follows: pressure is 0.1~0.8MPa, and temperature is 350~480
℃。
Washer N points are two sections, and the entrance washer lower section of mixture 31 of quench oil and oil gas, oil gas is in washer
In lower section uphill process, counter current contacting is carried out with washing oil 40, carries out gas-liquid separation simultaneously, the further dedusting of oil gas.Washer
Wash liquid distributed architecture, herringbone baffle or ring baffle or other structures for improving gas-liquid counter current contact is arranged in lower section, improves
Gas-liquid contact effect.What washer F lower section was isolated carries out solid-liquor separation containing solid mink cell focus 32 to liquid-solid separator P, isolates
It is low containing solid mink cell focus 33 enter heat exchanger O in exchange heat after return washer and enter washer bottom oil gas carry out adverse current gas
Liquid separation and dedusting, the low mink cell focus 41 admittedly that contains after heat exchange also can be used as product submitting.The Gao Hangu that liquid-solid separator P is isolated
Mink cell focus 34 to pre-reactor carries out freshening, has not only avoided not producing or producing low value less containing solid mink cell focus, but also can increase high value
Lightweight oil yield, greatly improves value-added content of product.The preferred sedimentation separation of liquid-solid separator P and cyclonic separation mode.Washing
The oil 35 isolated in the middle part of device partially forms 36 after extracting oil heat exchanger Q out and is back to washer top, with entrance washer F
The oil gas on top carries out second adverse current gas-liquid separation and dedusting；It is sent out as product 37 part.Cleaning solution is arranged in washer upper section
Body distributed architecture, separation tray or separation filler or other structures for improving gas-liquid counter current contact, improve gas-liquid contact effect.Through
It crosses two-phase seperation washing and isolates the submitting at the top of washer of cleaning oil gas 39 after mink cell focus, it is subsequent to may separate out without solid oil
With without solid carbonization gas, low without heavy oil content in solid oil, lightweight oil content is high, is conducive to following process into liquefied gas, vapour
The high value added products such as diesel oil or aromatic hydrocarbons, it is high without hydrogen in solid carbonization gas and methane content, it can extract high added value hydrogen
And methane product.For upper section extraction oil 43 after heat exchanger L takes heat, a part enters premixing device T, and another part returns to washing
Device or as output of products.External source 42 to washer lower section and oil gas can also be supplemented and carry out counter-current separation dedusting, external original
Expect 42 preferred following liquid or contains solid-liquid: heavy oil, residual oil, tar, slurry oil, gutter oil, waste oil, sump oil, shale oil etc..Washing
The operating condition of device N are as follows: pressure is 0.1~0.8MPa, and temperature is 80~400 DEG C；The operating condition of liquid-solid separator P are as follows: pressure
Power is 0.1~0.8MPa, and temperature is 80~400 DEG C；The operating condition of heat exchanger O are as follows: pressure is 0.1~2.0MPa, and temperature is
200~380 DEG C；The operating condition of heat exchanger Q are as follows: pressure is 0.1~1.5MPa, and temperature is 120~340 DEG C；The behaviour of heat exchanger U
Make condition are as follows: pressure is 0.1~1.5MPa, and temperature is 80~180 DEG C.
The equipment feature is preferred are as follows: carbonization reactor A length is 1~15 meter, pre-reactor F length is 1~10 meter,
Settler B length is 3~40 meters, and heater G length is 3~40 meters, and calcinatory J length is 3~30 meters, and washer N length is 5
~40 meters.
Embodiment
The present embodiment processes the honest oil-sand of Indonesia's cloth and tank field greasy filth using the device and method of the utility model.
The honest oil-sand of Indonesia's cloth and greasy filth main character used by the device are shown in Table 1, table 2 respectively.
The honest oil-sand raw material main character of 1 Indonesia's cloth of table
| Project | Unit | Numerical value | Remarks |
| Moisture content | Weight % | 2.4 | |
| Ash | Weight % | 52.6 | |
| Fugitive constituent | Weight % | 44.2 | |
| Sulfur content | Weight % | 0.8 |
Oil-sand raw material particle size range: partial size < 20cm；
2 greasy filth raw material main character of table
| Project | Unit | Numerical value | Remarks |
| Moisture content | Weight % | 6.0 | |
| Ash | Weight % | 21.0 | |
| Fugitive constituent | Weight % | 73.0 | |
| Sulfur content | Weight % | 0.5 |
Ratio=90%:10% (weight) of oil-sand and greasy filth.
(1) operating method
Device is as shown in Figure 1.
Raw material oil-sand 1-1 mix with the solid destructive distillation tailings 23 from heat collector broken by the crushing plant L
Form reaction feed 2.Broken solid material partial size is about less than 3 millimeters.
The premixing device T forms material 47 after mixing raw material greasy filth 1-2 with the extraction oil 46 that washer is isolated
Enter carbonization reactor as liquid form.The premixing device T is circulation mixing apparatus.
For the carbonization reactor A using fluidisation pattern, the pressure back-mixing structure with shunting, baffling function is arranged in inside,
Reaction feed 2, material 47 and the high-temperature material 15 from pre-reactor are rapidly achieved abundant back-mixing and mass-and heat-transfer.
The pre-reactor F by after settler B air lift destructive distillation tailings 12, from the heat supply tailings of heater G
16 and the Gao Hangu mink cell focus 34 from liquid-solid separator P mixed.The shunting of setting band, baffling function inside pre-reactor F
Back-mixing structure.
Level-one gas-solid separator C is set inside the settler B, so that into the reaction mass from A of settler B
3 realize the quick separating of oil gas and solid by level-one gas-solid separator C.Level-one gas-solid separator uses inverted L shape separator.Through
Cross two containing solid oil gas 4 by 6 entrance second level gas-solid separator D progress oil gas after settler that level-one gas-solid separator is isolated
Secondary dedusting, the oil gas 7 being greatly reduced by second level gas-solid separator D solid fines content is to quencher R, by second level gas-solid
The solid fines that separator D is isolated are back to settler.Second level gas-solid separator uses two stage cyclone separator, and it is heavy to be set to
It drops at the top of device.Enter settler lower part stripping section by the solid 5 that level-one gas-solid separator is isolated, passes through gas in stripping section
Distributor E injection gas stripping gas 29 (steam) removes entrained oil qi exhaustion in solid 9.Settler lower part is arranged herringbone baffle and improves gas
Gu the structure of counter current contacting.
The top heater G is solid settling section, and lower part is heat exchanging segment, and the solid 9 from settler is through overregulating
The boosted gas 10 (air) of valve a is promoted to 11 to mix changing with the high temperature body containing solid gas 21 from calcinatory J in heater
Heat.Heat exchanging segment uses turbulent fluidized bed pattern, and the gas after gas distributor I distribution improves the distribution of heat exchanging segment flow field.
After gas after heat exchange isolates most of solid fines into gas-solid separator H by forming 17 after the solid settling section of top
Gas 18 is sent out, and solid fines are back in the middle part of heater.Gas-solid separator H uses two stage cyclone separator, is set to heating
At the top of device G.
Destructive distillation tailings 20 from heater G enters calcinatory J by regulating valve d control and passes through gas distributor K's
Oxygen-containing gas 25 (air) carries out exothermic heat of reaction.
Calcinatory J is after the calcining tailings 22 of regulating valve e control discharge enters heat collector M heat recovery, a part circulation
To crushing plant, remainder is exported as product 24.The heat collector level-one takes heat+second level to take heat.The cooling of heat collector
Medium is water.
The promotion gas 13-1 is pyrolysis gas and promotion gas 13-2 is pyrolysis gas.
High-temperature oil gas 7 after second level gas-solid separator D isolates most of solid is to quencher R by from washer
The quench oil 38 isolated is cooling.
Washer N points are two sections, and the entrance washer lower section of mixture 31 of quench oil and oil gas, oil gas is in washer
In lower section uphill process, counter current contacting is carried out with washing oil 40, carries out gas-liquid separation simultaneously, the further dedusting of oil gas.Washer
Wash liquid distributed architecture is arranged in lower section, herringbone baffle improves the structure of gas-liquid counter current contact.What washer F lower section was isolated contains
Gu mink cell focus 32 carries out solid-liquor separation to liquid-solid separator P, the low mink cell focus 33 admittedly that contains isolated enters in heat exchanger O after heat exchange
It returns to washer and enters the oil gas progress adverse current gas-liquid separation and dedusting of washer bottom, it is low containing solid mink cell focus 41 after heat exchange
Also it can be used as product submitting.The Gao Hangu mink cell focus 34 that liquid-solid separator P is isolated to pre-reactor carries out freshening.Solid-liquor separation
Device P uses sedimentation separation mode.The oil 35 isolated in the middle part of washer partially forms 36 after extracting oil heat exchanger Q out and is back to
Washer top carries out second adverse current gas-liquid separation and dedusting with the oil gas for entering the top washer F；It is sent as product 37 part
Out.Wash liquid distributed architecture is arranged in washer upper section, separation tray improves the structure of gas-liquid counter current contact, improves gas-liquid contact
Effect.Cleaning oil gas 39 after mink cell focus is isolated in two-phase seperation washing is sent out at the top of washer.Upper section extraction oil 43
After heat exchanger L takes heat, a part enters premixing device T, and another part returns to washer or as output of products.
Prevailing operating conditions:
The operating condition of crushing plant L are as follows: pressure is 0.1~0.15MPa, and temperature is 50~80 DEG C.
The operating condition of premixing device T are as follows: pressure is 0.6~0.8MPa, and temperature is 80~120 DEG C.
Carbonization reactor A operating condition are as follows: pressure is 0.2~0.4MPa (G), and temperature is 480~520 DEG C, linear gas velocity
0.4~0.6 meter per second.
The operating condition of settler B are as follows: pressure is 0.2~0.4MPa (G), and temperature is 480~520 DEG C, upper gas line
Fast 0.1~0.3 meter per second.
Pre-reactor F operating condition are as follows: pressure is 0.2~0.4MPa (G), and temperature is 550~580 DEG C, linear gas velocity
0.5~0.7 meter per second.
Heater G operating condition are as follows: pressure is 0.2~0.4MPa (G), and temperature is 600~670 DEG C, linear gas velocity 0.1
~0.3 meter per second.
Calcinatory J operating condition are as follows: pressure is 0.25~0.45MPa (G), and temperature is 930~960 DEG C, linear gas velocity
0.4~0.6 meter per second.
The operating condition of heat collector are as follows: pressure is 0.15~1.0MPa, and temperature is 80~950 DEG C.
Quencher R operating condition are as follows: pressure is 0.2~0.4MPa (G), and temperature is 400~420 DEG C.
Washer N operating condition are as follows: pressure is 0.15~0.35MPa (G), and temperature is 120~380 DEG C.
Liquid-solid separator P operation condition are as follows: temperature is 280~320 DEG C.
The operating condition of heat exchanger O are as follows: pressure is 0.3~0.8MPa, and temperature is 280~360 DEG C.
The operating condition of heat exchanger Q are as follows: pressure is 0.5~1.5MPa, and temperature is 220~320 DEG C.
The operating condition of heat exchanger U are as follows: pressure is 0.1~1.5MPa, and temperature is 105~150 DEG C.
16~22 meter per second of level-one gas-solid separator inlet velocity.
18~24 meter per second of second level gas-solid separator inlet velocity.
18~24 meter per second of gas-solid separator H inlet velocity.
Carbonization reactor A length is 6 meters.
Pre-reactor F length is 8 meters.
Settler B length is 25 meters.
Heater G length is 24 meters.
Calcinatory J length is 16 meters.
Washer N length is 28 meters.
(2) product distribution:
2 product distribution of table
Remarks: it containing solid mink cell focus whole freshening, does not produce containing solid mink cell focus and intermediate extraction oil.
(3) product main character:
3 product oil gas of table (C4 following components) mainly forms
4 product oil gas of table (C4 or more component) simulation distillation data
| Weight % | Vapo(u)rizing temperature DEG C | Remarks |
| 5% | 95 | |
| 10% | 134 | |
| 30% | 218 | |
| 50% | 275 | |
| 70% | 314 | |
| 90% | 372 | |
| 95% | 405 |
Table 5 calcines tailings primary chemical composition
| Title | Weight % | Remarks |
| CaO | 66.4% | |
| SiO2 | 17.2% | |
| Al2O3 | 6.3% | |
| Na2O | 5.8% | |
| Fe2O3 | 2.7% | |
| K2O | 0.65% | |
| SrO | 0.28% |
It is incorporated herein by reference in all documents that the utility model refers to, just as each document quilt
It is individually recited as with reference to such.In addition, it should also be understood that, after having read the above-mentioned teaching content of the utility model, this field skill
Art personnel can make various changes or modifications the utility model, and such equivalent forms equally fall within the application appended claims
Book limited range.
Claims (10)
1. a kind of oil-sand and greasy filth comprehensive utilization device, which is characterized in that described device includes crushing plant (L), premixing device
(T), carbonization reactor (A), pre-reactor (F), settler (B), heater (G), calcinatory (J), heat collector (M), quencher
(R), washer (N), liquid-solid separator (P), heavy oil heat exchanger (O), middle section extraction oil heat exchanger (Q) and upper section extraction oil change
Hot device (U)；
Settler settling section setting up and down and stripping section；Including level-one gas-solid separator (C), second level gas-solid separator (D)
With gas distributor (E)；The level-one gas-solid separator (C) and second level gas-solid separator (D) belong to settling section, level-one gas-solid point
It is arranged inside settler from device (C), second level gas-solid separator (D) is arranged inside or outside settler；The gas distribution
Device (E) belongs to stripping section, and the lower part inside settler is arranged in；
The heater includes gas-solid separator (H) and gas distributor (I)；The gas-solid separator is arranged in heater body
Or it is external；The lower part of heater body is arranged in the gas distributor；
The calcinatory includes gas distributor (K)；The lower part inside calcinatory is arranged in the gas distributor (K)；
Wherein, crushing plant entrance is connected with heat collector outlet, and crushing plant outlet is connected with carbonization reactor entrance；Premix is set
Standby entrance is connected with the outlet of upper section extraction oil heat exchanger, and premixing device outlet is connected with carbonization reactor entrance；Carbonization reactor
Outlet is connected with the level-one gas-solid separator inside settler, and carbonization reactor entrance is set with crushing plant outlet, premix respectively
Standby outlet is connected with pre-reactor outlet；Pre-reactor entrance is connected with settler outlet, liquid-solid separator outlet respectively, pre- anti-
Device outlet is answered to be connected with carbonization reactor entrance；Settler lower part outlet is connected with pre-reactor, calorifier inlets respectively；Heating
Device lower part outlet is connected with pre-reactor and calcinatory entrance respectively；The gas distributor phase of calcinatory upper outlet and heater
Even, calcinatory lower part outlet is connected with heat collector entrance；
Second level gas-solid separator in settler is connected with quencher entrance, and quencher outlet is connected with washer bottom inlet；
Washer bottom is equipped with outlet and is connected with liquid-solid separator entrance；Liquid-solid separator outlet is changed with pre-reactor, mink cell focus respectively
Hot device entrance is connected；Mink cell focus heat exchanger exit is connected with washer lower part；Outlet is equipped in the middle part of washer to be connected with quencher；
Upper section extraction oil heat exchanger entrance and exit is connected in the middle part of washer and top respectively, and upper section is extracted out on oil heat exchanger also
It is connected equipped with outlet with premixing device；Middle section extract out oil heat exchanger entrance and exit respectively with the phase up and down in the middle part of washer
Even；And the entrance of middle section extraction oil heat exchanger is arranged in the connecting tube of washer and quencher.
2. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that
Settler lower part and heater are equipped with connecting tube, set regulating valve in connecting tube；
Settler lower part and pre-reactor are equipped with connecting tube, set regulating valve in connecting tube；
Heater lower part and pre-reactor are equipped with connecting tube, set regulating valve in connecting tube；
Heater lower part and calcinatory are equipped with connecting tube, set regulating valve in connecting tube；
Calcinatory lower part and heat collector are equipped with connecting tube, set regulating valve in connecting tube.
3. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that in the carbonization reactor optionally
Ground is equipped with external source entrance.
4. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that the crushing plant is equipped with original
Expect entrance.
5. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that the premixing device is equipped with original
Expect entrance.
6. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that the calcinatory, heater and
Settler is equipped with gas access.
7. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that the calcinatory is equipped with external
Fuel inlet and optional exotic high temperature gas access.
8. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that the heat collector is equipped with product
Delivery outlet.
9. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that the gas-solid separator is equipped with
Output of products mouth.
10. oil-sand as described in claim 1 and greasy filth comprehensive utilization device, which is characterized in that the heavy oil heat exchanger, in
Section extraction oil heat exchanger and upper section extraction oil heat exchanger are equipped with output of products mouth.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109385288A (en) * | 2018-12-13 | 2019-02-26 | 上海博申工程技术有限公司 | A kind of oil-sand and greasy filth method of comprehensive utilization and device |
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2018
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109385288A (en) * | 2018-12-13 | 2019-02-26 | 上海博申工程技术有限公司 | A kind of oil-sand and greasy filth method of comprehensive utilization and device |
| CN109385288B (en) * | 2018-12-13 | 2024-03-22 | 上海博申工程技术有限公司 | Comprehensive utilization method and device for oil sand and oil sludge |
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