CN105542826A

CN105542826A - Method for extracting oil from solid particle and heavy hydrocarbon self-contained stream

Info

Publication number: CN105542826A
Application number: CN201610028918.6A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Individual
Priority date: 2016-01-10
Filing date: 2016-01-10
Publication date: 2016-05-04

Abstract

The invention provides a method for extracting oil from a solid particle and heavy hydrocarbon self-contained stream. The method is suitable for a process for extracting oil from oil-bearing semi-coke during direct hydrogenation liquefaction of coal, and capable of improving the oil-solid separation efficiency. Based on the essential knowledge that oil-solid separation belongs to a process of entropy increase, the method has the following advantages: a conventional separation mode is changed fundamentally; a stream, which has the proper boiling point, heat stability and pressure as well as comes from the internal or external system for direct hydrogenation liquefaction of coal, is adopted for preparation of a gas heat carrier; and by adoption of fluidized bed cloud detonation flash evaporation, surface energy, heat energy and kinetic energy can be quickly transferred to a target material, so as to achieve a multi-dimensional entropy increase effect.

Description

The method of oil is extracted in the logistics of a kind of self-contained solid particulate and heavy hydrocarbon

Technical field

The present invention relates in the logistics of a kind of self-contained solid particulate and heavy hydrocarbon the method extracting oil; Particularly, the present invention relates in the logistics of a kind of self-contained solid particulate and Gao Fang heavy hydrocarbon the method extracting oil; More particularly, the present invention relates to a kind of containing porous carbon solid particulate and heavy hydrocarbon logistics in extract the method for oil; The present invention is suitable for the process of the oil-containing semicoke extraction oil that direct hydrogenation liquefaction of coal process exists, and can improve the solid separation efficiency of oil; Admittedly be separated based on oil and belong to this essence understanding of entropy increasing process, the present invention fundamentally changes existing clastotype, gaseous heat-carrier is prepared in the logistics that employing is suitable for from the boiling point in or beyond direct hydrogenation liquefaction of coal procedures system, thermostability is suitable for, pressure is suitable, adopt as " the quick-fried cloud flash distillation of fluidized-bed " mode, transmit surface energy, heat energy, kinetic energy fast to target material, realize multidimensional and increase entropy effect.

Background technology

Of the present invention

The present invention relates to the process GOP of the oil-containing semicoke extraction oil that direct hydrogenation liquefaction of coal process comprises.

Oil-containing semicoke extracts the process GOP of oil, and current universal method is divided into three steps substantially:

1. containing the vacuum flashing of heavy oil semicoke;

2. residual oil semicoke water vapour decompression air lift is contained after flash distillation;

3. the coking process of residual oil semicoke is contained after water vapour decompression air lift.

In direct hydrogenation liquefaction of coal process R10 and the direct liquefaction process of coal hydrogenation, the carbon skeleton do not liquefied is comprised in coal hydrogenation direct liquefaction reaction effluent R10P, ash content, the liquefaction semicoke that catalyzer etc. are formed, due to capillary action and reaction product, hydrogen supply agent retaining in liquefaction semicoke duct, liquefaction semicoke belongs to oil-containing semicoke, usually, oil separating recycling step is generated in the direct liquefaction of coal hydrogenation, at vacuum tower bottoms, obtain oil-containing semicoke, in order to improve the liquefied coal coil rate of recovery, be desirably in underpressure distillation separating step or the solid logistics of this oil of follow-up supplementary separating step (as oily step is put forward in the coking of the existing VACUUM TOWER BOTTOM dregs of fat) high efficiency separation, but due to semicoke " (surface-area is large for ultrafine powder, particle number is many), many pores, carbonaceous body, thermal conductivity is low " feature is natural is provided with that " capillary attraction power is strong, oil adsorptive power is strong, absorption internal surface area is huge, thermal conductivity is low ", and the last running of liquefied coal coil to belong to polycyclic aromatic hydrocarbon content high, and the macromole containing gum asphalt component, high viscosity hydrocarbon ils, " the oily Bao Gu of such a pair " oil is solid " binary thing composition, admittedly wrap oil " liquid-solid system, heating evaporation and or reduction vaporization reclaim heavy oil sepn process in, namely the condensed state attribute of the oil product of semicoke particle different positions must inconsistently differ greatly, substantially can be divided into 11 classes:

CTLHS-1A: the outside oil reservoir of semicoke outside surface oil reservoir, namely away from the side oil reservoir of semicoke solid, is called the external free oil phase of solid;

CTLHS-1B: namely the inside oil reservoir of semicoke outside surface oil reservoir is adsorbed in the side oil reservoir of semicoke solid, is called solid external surface constraint oil phase;

CTLHS-2A: the outside oil reservoir of the internal surface oil reservoir outside semicoke inner duct or near aperture, namely away from the side oil reservoir of semicoke solid, is called the free oil phase in solid aperture;

CTLHS-2B: namely the inside oil reservoir of the internal surface oil reservoir outside semicoke inner duct or near aperture is adsorbed in the side oil reservoir of semicoke solid, is called solid vent surface constraint oil phase;

CTLHS-3A: semicoke inner duct namely away from the side oil reservoir of semicoke solid, is called the semi-free oil phase of solid cell ends farthest away from the outside oil reservoir of the internal surface oil reservoir of orifice position; Liquid phase why is referred to as semi-free oil phase, because must be subject to the impact of semicoke solid wall surface molecule around;

CTLHS-3B: namely semicoke inner duct is adsorbed in the side oil reservoir of semicoke solid farthest away from the inside oil reservoir of the internal surface oil reservoir of orifice position, is called solid duct end surface strong constraint oil phase; Why be referred to as strong constraint oil phase, because this place's liquid phase must be subject to the impact of semicoke wall molecular solids around, " liquid phase adsorption field " that the high viscosity macromole hydrocarbon ils such as polycyclic aromatic hydrocarbons, colloid, bituminous matter being simultaneously enriched in semicoke wall solid around because of absorption defines makes strong constraint oil phase molecule have lower potential energy, must reduce the heat movement speed of strong constraint oil phase molecule;

CTLHS-4A: the outside oil reservoir of the internal surface oil reservoir of semicoke inner duct middle section position, namely away from the side oil reservoir of semicoke solid, is called the semi-free oil phase in stage casing, solid duct, the i.e. oil phase of locus between CTLHS-2A and CTLHS-3A;

CTLHS-4B: semicoke inner duct middle section position the inside oil reservoir of internal surface oil reservoir be namely adsorbed in the side oil reservoir of semicoke solid, be called surface, stage casing, solid duct strong constraint oil phase, i.e. the oil phase of locus between CTLHS-2B and CTLHS-3B;

CTLHS-5: caused potential close by structural collapse in semicoke inner duct and the liquefaction oil retained at enclosed space, be called solid tunnel collapse and close oil phase;

Oil phase is closed in the coking of CTLHS-6 duct: the liquefaction oil that the hydro carbons coking material generated because of high-temperature operation in semicoke inner duct blocks duct and retains at enclosed space, is called the coking of solid duct and closes oil phase;

CTLHS-7: because high-temperature operation is finally converted into the hydrocarbon ils of hydro carbons coking material in semicoke inner duct, is called coking predecessor hydrocarbon.

Below in conjunction with the condensed state attribute of the oil product of above-mentioned semicoke different positions, analyze the thermodynamics root of existing oily solid separation method weak effect.

Oil-containing semicoke extracts the vacuum flashing of oily process GOP, oily process is put forward in the flash distillation of water vapour air lift, coking, only as can be seen from its technology type namely, this is the transplanting to black petroleum products fractionation by distillation deep drawing technology, residuum coking technology, belongs to balance each other separation and chemical reaction isolation technique category.But thermomechanical analysis below will be pointed out, this will be a kind of congenital defect " technology newborn baby ", and it at all cannot the expectation of actualizing technology implementer, and therefore, before following this road, passerby must suffer defeat.

First the thermodynamics approach mutation analysis just without the separating of oil process VGOS of petroleum coal basic weight is as follows:

(1) vacuum flashing sepn process, water vapour air lift flash vaporization process adopt the entropy of the separation method that balances each other to subtract process

1. separate targets is wax oil, lightweight residual oil is separated with heavy oil residue;

If 2. the constant i.e. temperature of normal condition, pressure are constant, because two narrow fraction liquid phases more close to ideal solution and molecular potential lower, that is after being separated, total energy is lower, therefore overall sepn process belongs to entropy subtracts process, therefore sepn process belongs to the inverse process of spontaneous process mixing, for " evaporation+condensation " overall process, in high-temperature position T1 place, tower bottom input ENERGY E, then take out the condensation that ENERGY E realizes gas at low-temperature level T1 place, tower top, overall process forms entropy and subtracts process:

(E/T1)-(E/T2)＜0；

In said process, from aerodynamic point, it is propulsion source that tower bottom high-temperature position T1 inputs ENERGY E, and tower top low-temperature level T1 takes out ENERGY E and is manufacture negentropy; Gas phase is up is because the condensation process that tower top low-temperature level T1 takes out ENERGY E has manufactured gas-phase condensation low pressure area; Liquid phase is descending is because the traction of earth gravity;

3. according to boiling point order, multi-stage vaporizing is compared with once vaporizing from low to high, and final effect is, repeatedly more once vaporization separating effect is better in counter current contact vaporization; This is because under pure gas-to-liquid contact condition, the repeatedly counter current contact vaporization of multi-component liquid will build the temperature distribution field of more gradients;

(2) delayed coking sepn process balances each other that separation, a small amount of liquid-solid desorption are separated, the combination of Reaction Separation;

1. separate targets is lightweight residual oil and being separated of heavy oil residue, and gas is separated with other liquid-solid phase;

2. to input premised on large energy, meet the thermally splitting heat absorption of the heat absorption of light slag oil gasification and coking, realize gas solid separation, thermal condensation thermal discharge is less on the back burner;

3. inputting energy process (coking heater heat supply) is entropy increasing process;

If 4. normal condition is constant, STRENGTH ON COKE tower, the reaction of oil gas evaporation in coke drum, cracking into gas all absorbs amount of heat and belongs to entropy increasing process, but the molecule number of condensation coking minimizing process belongs to entropy and subtracts process, the entropy of its release of heat subtracts process and has the negative function that liquidates, and coking is reacted to belong to and developed from inside to outside, burnt core is that liquid oil encirclement is beneficial to heat transfer, and the condensation green coke heat release of kernel is beneficial to the radial temperature difference reducing green coke district; Coking aggregate performance is that entropy increases endothermic process, coker drum operation process institute heat requirement is brought into continuously by a large amount of high volume ratio hot gas thermal barrier entering coke drum bottom and (is noted, only account for a part for charging heat content), as energy transfer mode, a part is passed out by the high boiling component condensation heat release in charging, and one side point reduces temperature release heat energy by " gaseous fraction that lower both the components of boiling point that the lower component of uncooled boiling point, reaction generate form " through coke drum and passes out; In coke drum, along with green coke process advances, to early stage, the heat transmission resistance of institute's green coke charcoal constantly increases, and the sufficiently long time must be arranged for the heat energy that conducts heat, and namely heating time must be sufficient, at least will meet the needs of green coke process; Institute's green coke charcoal belongs to macrobead, and in fact before hydraulic decoking, in whole coke drum, coke solids only may be split into several pieces is exactly even overall one piece, and its granule number reaches only a few, and its entropy is extremely low.

Contrastively, carry out, the thermodynamics approach mutation analysis that the oil-containing semicoke of direct hydrogenation liquefaction of coal liquefaction process extracts oily process GOP is as follows:

(1) vacuum flashing sepn process, water vapour air lift flash vaporization process, comprise balance each other separation and the 2 kinds of sepn processes of liquid-solid desorption, is desorb, vaporizing to be separated accounts for leading entropy increasing process:

1. except wax oil, lightweight residual oil in free liquid phase are separated except SA with the vaporization between heavy oil residue, a large amount of separation tasks is the solid desorb of oil, vaporization is separated SB;

If 2. normal condition is constant, based on aforementioned, SA overall process belongs to entropy and subtracts process;

If normal condition is constant, because liquid-solid two-phase ADSORPTION STATE potential energy is lower, the desorption vaporescence terminating absorption relation will have higher potential energy, SB overall process belongs to entropy increasing process, basic form is " heat absorption, desorb, vaporization ", input energy is entropy increasing process, consider that semicoke extracts solid-liquid part by weight in the raw material of oily process GOP and is about 0.5 ~ 1.5, be generally 0.7 ~ 1.2, the absorption sea bottom surface of the internal surface formation of semicoke ultrafine powder defines huge entropy to adsorbed oil and subtracts (exothermic effect of adsorption process), therefore solid " the heat absorption of the oil of GOP, desorb, vaporization " sepn process belongs to the leading entropy increasing process of SB, before overall " heat absorption, desorb, the vaporization " task of end, do not wish, also should not occur that causing " reverse operating " of negative effect namely to form entropy subtracts process (such as temperature-fall period),

This point, compared with the flash separation of sepn process VGOS, it is contrary in itself that the thermodynamics of approach points to;

3. vaporize step by step from low to high according to boiling point order and once vaporize widely different; To vaporize step by step residual liquid phase, because molecular weight is larger, wall adsorption power is larger, viscosity is larger, thermal condensation temperature is lower, makes vaporization escape difficulty increase;

(2) delayed coking sepn process, belonging to the anabolic process be separated of the separation that balances each other, liquid-solid desorption vaporization separations, porous carbon particle aggregation body heat transferring, gas and other liquid-solid phase, is the combination of separation, a large amount of liquid-solid desorption separation, Reaction Separation of balancing each other:

1. the diffusional resistance that main body separate targets is the desorb of ADSORPTION STATE oil in semicoke inner duct, inner duct diffusion is escaped, formed through inaccessible obstacle, enters gas phase main body and is recovered;

Secondary separate targets is lightweight residual oil to be separated with other liquid-solid phase with being separated of heavy oil residue, gas;

2. to input premised on large energy, meet the thermally splitting heat absorption of the heat absorption of light slag oil gasification and coking, realize solid-liquor separation, thermal condensation thermal discharge is less on the back burner;

If 4. normal condition is constant, STRENGTH ON COKE tower or coking device, the reaction of oil gas evaporation in coke drum, cracking into gas all absorbs amount of heat and belongs to entropy increasing process, but the molecule number of condensation coking minimizing process belongs to entropy subtracts process, and the entropy of its release of heat subtracts process and has the negative function that liquidates;

But because the hole inner fluid being hidden in the inside, duct of burnt grain forms porous semicoke solid bag oil form, and semicoke poor thermal conductivity forms the larger temperature difference distribution of semicoke particle radial direction, a large amount of semicoke ultrafine particulate solid assembles the thermodynamic barrier that (having low surface energy) forms biography process in outer heat together, as cannot high dispersing semicoke particle (have higher surface energy, more fluid diffusion channels mouth), even if there have a large amount of high specific heat gaseous heat-carriers to continue conveying heat energy to be also of no avail;

The coking of the oil product in semicoke duct, not only obtain heat energy difficulty, even if complete pyrogenic reaction, also following 2 consequences must be caused: first, pyrogenic reaction heat absorption causes semicoke internal surface coking district temperature to reduce rapidly, although small molecules product still can be escaped and be left semicoke duct, local area and neighbouring in, macromole high boiling component be more difficult to vaporization; The second, a large amount of coking causes semicoke inner duct to block, and facilitates the coking of CTLHS-6 duct to close oil phase;

In coke drum or coking device, along with green coke process advances, to early stage, the heat transmission resistance of institute's green coke charcoal constantly increases, and the sufficiently long time must be arranged for the heat energy that conducts heat, and namely heating time must be sufficient, at least will meet the needs of green coke process;

" liquid phase molecule thermal condensation green coke " mechanism is belonged to different from the delayed coking green coke of petroleum residual oil, the ultrafine powder semicoke of the coking of process GOP is from raw material, and become key possibility without strong chemical reaction between ultrafine powder semicoke, only has several forthright collision particle, because the residual oil molecule coking integrated process on surface can be combined into one " linker ", therefore, in essence, under the condition of input effective surface merit, the coking of process GOP, its green coke charcoal should belong to little, microparticle, its granule number is more, its entropy is higher, particle heat absorption will be beneficial to, be beneficial to the micromolecular escape of oil gas in particle,

If 5. consider because semicoke superficial attractive forces, cause same residual oil molecule vaporization temperature value inevitable higher than residual oil molecule vaporization temperature same in free liquid phase, this vaporization temperature increases and forms additional boiling point increment DBT, the vaporescence of same oil product molecule can increase considerably because of its thermal condensation coking speed of increase of vaporization temperature, and this effect too increases separation resistance.

Table 1 be sepn process VGOS and semicoke extract oily process GOP thermodynamics approach change analytical results gather.

As can be seen from Table 1, there is essential difference in two processes:

1. petroleum residual oil flash separation belongs to entropy and subtracts process;

Semicoke extracts oil flash sepn process and belongs to entropy increasing process;

2. the process that petroleum residual oil coking sepn process to belong in liquid phase green coke from inside to outside, readily conducts heat, few, the overall entropy increment of coke granule number is less;

The coking sepn process of semicoke extraction oil belongs to green coke in semicoke hole, difficulty is conducted heat, coke granule number is extremely many, there is the process that oil phase is closed in the coking of CTLHS-6 duct, semicoke surface oil molecule boiling point uprises, overall entropy increment is larger.

Foregoing description is a kind of comparative analysis language, but substantially realistic.

As can be seen from above contrast, by the isolation technique (flash distillation, water vapour air lift, coking) without the separating of oil process VGOS of petroleum coal basic weight, transplant the process GOP being used in oil-containing semicoke extraction oil and there is very big blindness, constitute the gross mistake of thermodynamics approach directive property, its separating effect extreme difference is inevitable.

As seen from the above analysis, coking step exist be difficult to eliminate " raw material contain magnanimity ultra-fine semicoke particle thus solid entropy greatly, magnanimity internal surface area absorption residual oil thus residual oil molecular potential is extremely low, heat transfer difficult " etc. intrinsic solid height entropy, the low entropy attribute of oil phase of raw material, improve the best solution of oil-containing semicoke coking separation efficiency, improve the separating effect of its source step and vacuum distillation process exactly, the oil eliminating or weaken coking step is separated task or refiltered oil effect admittedly.

The analytical results that table 1 sepn process VGOS and semicoke extract the thermodynamics approach change of oily process GOP gathers

Below analyze the entropy that existing oil-containing semicoke extracts the flash vaporization process of the conventional vacuum tower of oily process GOP, water vapour air lift process exists and subtract effect and root thereof, and then propose the present invention program:

1. the flash vaporization process in vacuum distillation tower, such as from upstream valve or furnace outlet to the course of conveying of vacuum distillation tower flash zone, gasify mutually because pressure reduces initiation solution, this process causes the reduction of liquidus temperature, this is a step producing that residual liquid phase entropy subtracts effect, is unfavorable for subsequent evaporation;

This illustrates, raw material needs to carry more heat energy, solid namely in the charging of existing conventional sepn process separation column hydrocarbon/ratio too low, hot logistics capacity should be increased, reduce flash vaporization point reduction amplitude;

2. in the water vapour air lift flash vaporization process in vacuum distillation tower, because water vapour volumetric heat capacity amount is extremely low, the main quick cooling heat release relying on liquid phase of oil product flash of steam caloric receptivity, this process causes liquidus temperature to reduce, this is also a step producing that residual liquid phase entropy subtracts effect, is unfavorable for subsequent evaporation;

Water vapour is as stripping medium, and its volumetric heat capacity is too low; In conventional theory, the water vapour air lift in vacuum distillation tower belongs to final step, does not also arrange the process of other input heat energy;

This illustrates, stripping medium should change to the large suitable material of volumetric heat capacity; Or arrange suitable delivery of energy step;

3. the water vapour air lift flash vaporization process in vacuum distillation tower, usually the multistage air lift flash distillation of polylith column plate is belonged to, the process that moves downward of oil-containing semicoke cause wherein raffinate molecule according to boiling point order stepped evaporation from low to high, the air lift degree of depth is more and more higher, contained by semicoke, the molecular weight of liquid is increasing, viscosity is increasing, in addition temperature is more and more lower, its evaporation difficulty rises rapidly, this process causes liquid phase and solid phase adsorption power to become large, this is also a step (liquid phase purity raising producing that residual liquid phase entropy subtracts effect, but liquid-solid adsorption power becomes large), be unfavorable for subsequent evaporation,

Water vapour air lift flash vaporization process in vacuum distillation tower, multistage air lift flash distillation, no matter adopt tray column or packing tower, all do not consider input surface merit, the space difference of elevation declined due to liquid is less, and transform gravitational energy gained kinetic energy increment is too little, and part gravity also by the gaseous stream that rises the direction of transmitting upwards lift or drag power offset, thus effectively cannot expand semicoke particle dispersion to increase surface-area, namely cannot expand heat transfer area and flash distillation area; This explanation, the flash distillation of multi-stage countercurrent air lift, at least there is above-mentioned defect, counter current contact number of times should reduce, be preferably single flash distillation, be even preferably and flow with or the atomization of cross-flow, heating, flash distillation, flow field be separated, or the mode of operation being beneficial to the dispersion of strengthening semicoke, gas-particle heat transfer, gas solid separation of any appropriate, can be the combination of effective traditional unit operations, a kind of suitable mode be fluid bed dispersion solid, fluidized-bed, gas-solid centrifugation combination;

In order to obtain the desorption efficiency of high boiling component to greatest extent, just must suppress the effect of " going light constituent to stay heavy constituent " of classification flash distillation to greatest extent, namely cut down multistage flash evaporation to greatest extent namely to need to shorten to greatest extent " flash vaporization process time ", based on above-mentioned conceptual understanding, the present invention's imagination shortens " flash vaporization process cycle " to greatest extent, form " quick direct heating and rapid flash " integrated process to greatest extent, realize " the theoretical flash distillation of single-stage " of thermodynamics space minimization, utilize the flash of steam gained gas of the low boiling component of semicoke granule interior as sweeping gas, " from inside to outside " the hydrocarbon ils liquid phase particularly high boiling hydrocarbon fluid phase in semicoke duct is impacted, formed " quick-fried blow effect " of naphtha steam blowout heavy oil liquid,

Quick-friedly blow effect, naturally quick heat supply is required, this illustrates, needs the heat-carrying gas that use temperature is high, volumetric heat capacity amount is large, pressure is high to provide dispersion mechanical work, heat energy to semicoke, then utilizes the motion of high velocity air to arrange suitable method such as centrifugal separation processes etc. and complete gas solid separation.

So far, the present invention has proposed principle technical scheme, uses the high temperature heat-carrying gas that volumetric heat capacity is large, rapid dispersion, heating oil-containing semicoke raw material, and realize the oil product vaporization in semicoke hole, namely need to form " quick-fried cloud flash distillation ", its functional characteristics is:

1. " quick-fried ", refer to and complete surface work input, heat energy input with the extremely short time, suppress multistage flash evaporation effect, strengthening " quick-fried blow effect "; Clearly, its implication is exactly that hint uses suitable high temperature, high volumetric heat capacity gas, direct fluidisation, heating oil-containing semicoke, and a kind of suitable mode is fluidized-bed type of heating;

2. " cloud ", oil-containing semicoke preferably first discretize or cloud and mist is as far as possible referred to; Clearly, its implication is exactly that hint hot gas impacts oil-containing semicoke, provides surface energy;

3. " flash distillation ", the natural consequence referring to oil-containing semicoke " Cheng Yun " fast endothermic is afterwards exactly efficient " flash distillation ".

" quick-fried cloud flash distillation " of the present invention, its preferred plan is " quick-fried cloud thermal shocking flash distillation " naturally, cloud and thermal shocking two steps are dispersed in order to strengthen, two-way heat-carrying gas can be adopted or be divided into two-way to perform dispersion, heating tasks respectively in heat-carrying gas, quick-fried cloud thermal shocking flash distillation is decomposed into 2 or multiple series connection steps and carries out, such as " quick-fried cloud+thermal shocking flash distillation ", " quick-fried cloud+thermal shocking+flash distillation ", " quick-fried cloud+thermal shocking+flash distillation+gas solid separation ".

Certainly can expand this thinking, be formed multistage " quick-fried cloud flash distillation ".

So far, can find out, for fluid bed dispersion solid, fluidized-bed heating, step-down flash distillation, gas-solid centrifugation array mode, heat-carrying gas of the present invention, at least has multi-functional as described below:

1. solid dispersal gas, as the dispensing implement of semicoke particle, surface work is done to oil-containing semicoke and improves oil-containing semicoke surface energy, to oil-containing semicoke, there is relative high speed, kinetic energy is transmitted to oil-containing semicoke particle when meeting with oil-containing semicoke, high-speed gas distribution field is formed to oil-containing semicoke, relevant hydraulic factors comprise dispersed gas flow velocity, the flow direction, totally spray flow field;

2. heat solid heat-carrying gas, provides the heat energy of high volumetric heat capacity, and its temperature T2 is higher than oil-containing semicoke service temperature T1;

Overall injection flow field determines heat transfer process simultaneously, also determine temperature distribution field;

3. carry kinetic energy gas, transmit kinetic energy to semicoke particle, make solid high-speed motion, leave dispersion, primary heat transfer functional zone, ensure non-stop run;

4. gas solid separation flow field control gas, after flash distillation the gentle body of semicoke sepn process in, heat-carrying gas is in fact the flow field control power gas of sepn process.

Namely heat-carrying aerodynamics divergent function to thermodynamics heat-carrying function to the implication of heat-carrying gas component normal boiling point is, the normal boiling point of heat-carrying gas component must reclaim the normal boiling point of limit of the objective hydrocarbon component lower than oil-containing semicoke, reason is as follows:

1. heat-carrying gas, specify that it is gas phase in whole sepn process phase, therefore not only at the end of separating step, (working pressure is minimum, the end workflow position that temperature is minimum) heat-carrying gas is gas phase, when contacting with oil-containing semicoke, (working pressure is higher, the middle workflow position that temperature is higher) be gas phase, and (working pressure is the highest at the pre-distributed process as dispersed gas " formation flow field ", the initial workflow position that temperature is the highest) also must be preferably gas phase, temperature is reduced when being converted into heat-carrying gas to prevent the dispersed gas containing liquid phase, namely as being also preferably gas phase during dispersed gas,

2. in addition, this also prevents droplet impact in dispersed gas, destroys required by discrete part.

Assuming that the normal boiling point that oil-containing semicoke reclaims limit of the objective component is 540 DEG C, table 2 lists the pressure-boiling point data of potential similar boiling points heat-carrying gas hydro carbons.

Table 2 is the pressure-boiling point data of potential similar boiling points heat-carrying gas hydro carbons, for analyzing the pressure of potential similar boiling points hydro carbons to the impact of boiling point.Table 3 is the limit operation pressure-boiling point data of potential similar boiling points heat-carrying gas hydro carbons, for analyzing the gas phase operation pressure range of potential similar boiling points hydro carbons.

Pressure-boiling point the data of the similar boiling points heat-carrying gas hydro carbons that table 2 is potential

Limit operation pressure-boiling point the data of the similar boiling points heat-carrying gas hydro carbons that table 3 is potential

Below analyze suitable heat-carrying gas component.

The present invention abandons water vapour stripping medium, and replace the heat-carrying gas KTEG of high volumetric heat capacity, it must possess following characteristics:

, should not there is chemical reaction with oil-containing semicoke contained oil in 1. component contained by heat-carrying gas KTEG, should not affect the purposes from oil-containing semicoke refiltered oil with refiltered oil after mixing, and in fact this indicate component necessarily conventional liquid hydrocarbon contained by heat-carrying gas KTEG;

2. component contained by heat-carrying gas KTEG, and the adsorptive power between semicoke, should lower than or far below the oil coke adsorptive power of coal liquefaction products oil-containing semicoke, this is the basic demand to stripping medium, in fact this indicate that the polarity of component contained by heat-carrying gas KTEG at least should be weaker than coal liquefaction products heavy oil R10V, preferably as far as possible close to neutral;

3. the normal boiling point BSBPT of component contained by heat-carrying gas KTEG can not be too high, difference BSDT should be there is compared with the normal boiling point RLBPT of oil-containing semicoke contained oil, definition BSDT=RLBPT-BSBPT, BSDT should at least low go out a certain radix Temperature Difference Ratio as usually low go out 50 DEG C, low go out 100 DEG C, preferably low go out 200 DEG C, object is to prevent component contained by heat-carrying gas KTEG from being adsorbed in a large number by semicoke, form " peach is stiff for Lee " and cannot improve oily yield, in fact this indicate the boiling point higher limit of component contained by heat-carrying gas KTEG; Usual coal liquefaction products heavy oil R10V initial boiling point is 480 ~ 510 DEG C, so the normal boiling point BSBPT of heat-carrying gas KTEG, usually should not higher than 310 ~ 410 DEG C, and this is about the same in carbon 17 ~ carbon 25 hydro carbons;

4. the boiling point of component contained by heat-carrying gas KTEG should the normal boiling point BSBPT of component contained by too low i.e. heat-carrying gas KTEG can not be too low, usually, after heat-carrying gas KTEG completes heat supply gas stripping, finally must realize liquefaction, to process further or to recycle through condensation process LU; In condensation process LU, the heat energy that heat-carrying gas KTEG carries will be converted into low-temperature heat energy, and in order to reduce process energy consumption and energy level loss, should improve the potential temperature of condensation process LU heat release as far as possible, in fact this indicate the condensation point lower value of component contained by heat-carrying gas KTEG;

Heat-carrying gas KTEG, at least can liquefy under normal pressure and temperature, i.e. carbon number >=5 i.e. the carbon 5 of heat-carrying gas KTEG institute hydrocarbon components and more heavy hydrocarbons thereof; In order to make condensation process LU heat release be used effectively, its normal pressure liquefaction temperature should not lower than 160 DEG C, and this is about the same in the normal boiling point of carbon 10 hydro carbons.

Above analytic explanation, usually, the suitable ingredients of heat-carrying gas KTEG is the hydro carbons of C10 ~ C17 or C10 ~ C25, and namely normal boiling point is about the hydrocarbon-fraction of 160 ~ 310 DEG C or 160 ~ 410 DEG C, substantially can be divided into following two kinds:

1. normal boiling point is about the solar oil cut of 160 ~ 250 DEG C;

2. normal boiling point is about heavy gas oil, the light wax oil mixed fraction KBS of 250 ~ 410 DEG C.

If select the gasoline fraction hydro carbons of C5 ~ C10 to be used as heat-carrying gas KTEG, its shortcoming is:

1. compared with the reference gas thermal barrier KBS of C10 ~ C25 hydro carbons, under temperature, pressure the same terms, about 50% or lower of KBS is only because molecular weight is little, volumetric heat capacity is about about 50% or lower of KBS volumetric heat capacity, volumetric flow rate 2 times that are about KBS volumetric flow rate or more when carrying equivalent heat energy;

2. the collision task number of times of quick-fried cloud flash vaporization process " oil-containing semicoke and heated carrier gas component " at least needs for KBS about 2 times that collide task number of times or more, by requiring to extend the gas-solid mixing time, increasing dispersion collision spatial volume, is unfavorable factor;

3. heat-carrying gas KTEG volumetric flow rate is 2 times of KBS volumetric flow rate or more, will increase the Pressure Drop of identical device system, and increase pressure consumption, and for the present invention that expectation realizes rapid flash, this is the unfavorable factor affecting separating effect.

As for the part by weight of heat-carrying gas and oil-containing semicoke, set according to detailed process.

Below analyze suitable heat-carrying gas source.

The suitable source of heat-carrying gas can be the hydrocarbon stream comprised from the direct liquefaction process of coal hydrogenation, also can be from the hydrocarbon stream outside the direct liquefaction process of coal hydrogenation:

1. the sepn process gained hydrocarbon stream of the direct liquefaction reaction effluent of coal hydrogenation;

2. the hydrogen supply agent logistics of the direct liquefaction reaction feed of coal hydrogenation or its separated stream or its diverted stream is used as;

3. the hydrogenation upgrading reaction process feed hydrocarbon logistics of coal hydrogenation direct liquefaction reaction effluent gained hydrocarbon ils is separated;

4. well heater as process furnace and vacuum fractionation process as vacuum distillation tower between the heat-carrying gas that recycles, circulation experience " process furnace gasification, quick-fried cloud flash distillation heat supply, vacuum distillation tower fractionation, heat-carrying air cooling solidifying, heat medium oil pressurize and return process furnace " process, cause heating agent condensation to be gone bad to prevent circulating-heating and affect air lift effect, certainly can controlled circulation heated time, constantly substitute discharge heating agent;

5. the hydrocarbon stream outside direct hydrogenation liquefaction of coal liquefaction process.

The method of the invention has no report.

Therefore, the present invention first object is the method extracting oil in the logistics of a kind of self-contained solid particulate of proposition and heavy hydrocarbon.

The present invention second object is the method extracting oil in the logistics of a kind of self-contained solid particulate of proposition and Gao Fang heavy hydrocarbon.

The present invention the 3rd object be to propose a kind of containing porous carbon solid particulate and heavy hydrocarbon logistics in extract the method for oil.

Summary of the invention

Extract the method for oil in the logistics of a kind of self-contained solid particulate of the present invention and heavy hydrocarbon, it is characterized in that comprising following steps:

(1) at the first vaporization separate part S1, service temperature be T1 containing flow C F01 and the service temperature of solid particulate and the heavy hydrocarbon heat-carrying gas KTEG that is T2 complete contact at least one times after be separated into may gas stream S1V containing solid and at least contain the logistics S1SL of solid particulate;

At the first vaporization separate part S1, the vaporization of hydro carbons at least partially in flow C F01 enters in gas S1V;

Heat-carrying gas KTEG service temperature T2 is higher than flow C F01 service temperature T1;

The gross weight WRC-S1V of the conventional liquid hydrocarbon in logistics S1V, more than the gross weight WRC-KTEG of the conventional liquid hydrocarbon in heat-carrying gas KTEG;

The gross weight WRC-S1SL of the conventional liquid hydrocarbon in logistics S1SL, is less than the gross weight WRC-CF01 of the conventional liquid hydrocarbon in flow C F01;

(2) hydrocarbon stream HPF is obtained at recycling step S2, separated stream S1V.

The present invention, the boiling temperature relationship of flow C F01 and heat-carrying gas KTEG, the 1st kind of scheme is:

(1) 50% of conventional liquid hydrocarbon distillate a normal boiling point temperature CF01-NBP50 in flow C F01, deduct 50% of conventional liquid hydrocarbon in heat-carrying gas KTEG and distillate a normal boiling point temperature KTEG-NBP50 gained temperature gap DT1 and be greater than 50 DEG C.

The present invention, the boiling temperature relationship of flow C F01 and heat-carrying gas KTEG, the 2nd kind of scheme is:

(1) 50% of conventional liquid hydrocarbon distillate a normal boiling point temperature CF01-NBP50 in flow C F01, deduct 50% of conventional liquid hydrocarbon in heat-carrying gas KTEG and distillate a normal boiling point temperature KTEG-NBP50 gained temperature gap DT1 and be greater than 100 DEG C;

50% of conventional liquid hydrocarbon in flow C F01 distillates a normal boiling point temperature CF01-NBP50, deducts 85% of the conventional liquid hydrocarbon in heat-carrying gas KTEG and distillates a normal boiling point temperature KTEG-NBP85 gained temperature gap DT2 and be greater than 50 DEG C.

The present invention, the boiling temperature relationship of flow C F01 and heat-carrying gas KTEG, the 3rd kind of scheme is:

(1) 50% of conventional liquid hydrocarbon distillate a normal boiling point temperature CF01-NBP50 in flow C F01, deduct 50% of conventional liquid hydrocarbon in heat-carrying gas KTEG and distillate a normal boiling point temperature KTEG-NBP50 gained temperature gap DT1 and be greater than 200 DEG C;

50% of conventional liquid hydrocarbon in flow C F01 distillates a normal boiling point temperature CF01-NBP50, deducts 85% of the conventional liquid hydrocarbon in heat-carrying gas KTEG and distillates a normal boiling point temperature KTEG-NBP85 gained temperature gap DT2 and be greater than 100 DEG C.

The present invention, can obtain different hydrocarbon stream HPF1 and HPF2 of at least two boiling ranges at recycling step S2, separated stream S1V;

Hydrocarbon stream HPF1 comprises the most of conventional liquid hydrocarbon from heat-carrying gas KTEG in logistics S1V;

Hydrocarbon stream HPF2 comprises the most of conventional liquid hydrocarbon from flow C F01 in logistics S1V.

The present invention, obtains the hydrocarbon liquid phase logistics HPF9S containing solid at recycling step S2, separated stream S1V, and its whereabouts can be selected from:

1. logistics HPF9S mixes with logistics S1SL;

2. logistics HPF9S contacts with heat-carrying gas KTEG;

3. logistics HPF9S contacts with flow C F01.

4. logistics HPF9S with return the first vaporization separate part S1 and contact with process stream, the vaporization of hydro carbons at least partially in logistics HPF9S enters in gas S1V.

The present invention, at the first vaporization separate part S1, usually, the most of normal boiling point in flow C F01 is lower than 480 DEG C or lower than 500 DEG C or lower than 520 DEG C or lower than 540 DEG C or enter in gas S1V lower than the hydro carbons vaporization of 555 DEG C.

The present invention, at the first vaporization separate part S1, usually, logistics S1SL is that the part by weight defining the conventional liquid hydrocarbon in logistics S1SL is K99, K99≤0.50 or≤0.40 or≤0.30 or≤0.20 or≤0.10 containing solid, logistics containing conventional liquid hydrocarbon.

The present invention, usually, containing the flow C F01 of solid particulate and heavy hydrocarbon, is selected from the one in following materials or 2 kinds or several:

1. containing the middle coalite tar of solid particulate or its distillate or its hot procedure or its hydrogenation process gained oil product; Described hot procedure comprises coking, catalytic cracking process, catalytic pyrolysis process, visbreaking process, thermal cracking process; Described hydrogenation process comprises unifining process, hydrocracking process, heat from hydrogenation cracking process, hydro-upgrading process;

2. containing the coal-tar heavy oil of solid particulate or its distillate or its hot procedure or its hydrogenation process gained oil product;

3. containing the direct hydrogenation liquefaction of coal process gained Coal Liquefaction oil of solid particulate or its distillate or its hot procedure or its follow-up hydrogenation process gained oil product;

4. containing the shale oil of solid particulate or its distillate or its hot procedure or its hydrogenation process gained oil product;

5. containing tar sand basic weight oil or its hot procedure or its hydrogenation process gained oil product of solid particulate;

6. containing ethylene cracking tar or its hydrogenation process gained oil product of solid particulate;

7. containing petroleum base wax oil thermal cracking tars or its hydrogenation process gained oil product of solid particulate;

8. containing petroleum based heavy fuel oils hot procedure gained heavy oil fraction product or its hydrogenation process gained oil product of solid particulate;

9. containing solid particulate other aromatic hydrocarbons weight content higher than 35% gluey pitch shape composition weight content higher than 10% hydrocarbon ils or its hydrogenation process gained oil product.

The present invention, usually, containing the flow C F01 of solid particulate and heavy hydrocarbon, described solid particulate be selected from following in one or 2 kinds or several:

1. direct hydrogenation liquefaction of coal process gained semicoke particle;

2. granules of catalyst;

3. iron rust particle;

4. particles of inorganic material;

5. the solid particulate entered in coal tar of coking of coal process generation;

6. from the product solid particle of hydro carbons thermal condensation process;

7. from the solid particulate of shale;

8. from the solid particulate of oil-sand;

9. other is present in the particle in flow C F01.

The present invention, at the first vaporization separate part S1, the gross weight WRC-KTEG of the conventional liquid hydrocarbon in heat-carrying gas KTEG is defined as KWW divided by the gross weight WRC-CF01 of the conventional liquid hydrocarbon in flow C F01, i.e. KWW=(WRC-KTEG)/(WRC-CF01), KWW is generally 0.01 ~ 100, is generally 1.0 ~ 20.

The present invention, at the first vaporization separate part S1, the gross weight WRC-KTEG of the conventional liquid hydrocarbon in heat-carrying gas KTEG is defined as KWT divided by the gross weight WT-CF01 of flow C F01, i.e. KWT=(WRC-KTEG)/(WT-CF01), KWT is generally 0.01 ~ 40, is generally 2.0 ~ 5.

The present invention, usually, at the first vaporization separate part S1, containing the flow C F01 of solid particulate and heavy hydrocarbon, for containing the direct hydrogenation liquefaction of coal process gained direct hydrogenation liquefaction of coal oil of solid particulate or its distillate or its hot procedure gained oil product;

Described direct hydrogenation liquefaction of coal process, refers to coal and molecule hydrogen for raw material, hydrocarbon ils or be rich in hydrogen supply agent hydrocarbon ils existence condition under, coal directly comprises the reaction process of the hydrogenation liquefaction of carbon-carbon bond thermally splitting.

The present invention, generally, (1) at the first vaporization separate part S1, containing the flow C F01 of solid particulate and heavy hydrocarbon, for containing the direct hydrogenation liquefaction of coal process gained Coal Liquefaction oil of solid particulate or its distillate or its hot procedure gained oil product;

Described direct hydrogenation liquefaction of coal process, refer to coal and molecule hydrogen as raw material, hydrocarbon ils or be rich in hydrogen supply agent hydrocarbon ils existence condition under, under hydrogenation catalyst existence condition, coal directly comprises the reaction process of the hydrogenation liquefaction of carbon-carbon bond thermally splitting.

The present invention, usually, heat-carrying gas KTEG, is selected from the one in following materials or 2 kinds or several:

1. heat-carrying gas KTEG, with flow C F01 from same logistics F00;

Be separated organic stream F00, obtain heat-carrying gas KTEG and flow C F01;

2. heat-carrying gas KTEG, the logistics F00 produced from same hydrogenation process R10 with flow C F01;

Separated stream F00, obtains heat-carrying gas KTEG and flow C F01;

3. heat-carrying gas KTEG, finally as the feed stream FTOAFU of process AFU;

At the first vaporization separate part S1, enter in logistics S1V after heat-carrying gas KTEG contacts with flow C F01;

Hydrocarbon ils HPF-TOAFU is obtained at recycling step S2, separated stream S1V; Hydrocarbon ils HPF-TOAFU contains the most of conventional liquid hydrocarbon in heat-carrying gas KTEG;

Hydrocarbon ils HPF-TOAFU enters process AFU;

4. heat-carrying gas KTEG is the feed stream FTOAFU of process AFU;

Hydrocarbon ils HPF-TOAFU is obtained at recycling step S2, separated stream S1V; Hydrocarbon ils HPF-TOAFU contains the conventional liquid hydrocarbon of more than 80% in heat-carrying gas KTEG;

Hydrocarbon ils HPF-TOAFU enters process AFU;

5. heat-carrying gas KTEG is the feed stream FTOAFU of process AFU;

Hydrocarbon ils HPF-TOAFU is obtained at recycling step S2, separated stream S1V; Hydrocarbon ils HPF-TOAFU contains the conventional liquid hydrocarbon of more than 90% in heat-carrying gas KTEG;

Hydrocarbon ils HPF-TOAFU enters process AFU;

6. heat-carrying gas KTEG, enters associating course of processing AFSH after mixing with the hydrocarbon component based on flow C F01;

Hydrocarbon ils HPF-TOAFSH is obtained at recycling step S2, separated stream S1V; Hydrocarbon ils HPF-TOAFSH contains the most of conventional liquid hydrocarbon in heat-carrying gas KTEG and the close component of boiling point from flow C F01;

Hydrocarbon ils HPF-TOAFU enters associating course of processing AFSH;

7. heat-carrying gas KTEG is the hydrocarbon ils HPF-RP that recycling step S2 separated stream S1V obtains;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

Hydrocarbon ils HPF-RP absorbs after heat through heat-processed HX01 and is converted into hot logistics HPF-RP-E at least partially, and hot logistics HPF-RP-E recycles as heat-carrying gas KTEG at least partially.

The present invention, at the first vaporization separate part S1, containing the flow C F01 of solid particulate and heavy hydrocarbon, for containing solid particulate Coal Liquefaction process R10 gained Coal Liquefaction oil or its distillate time, usually, heat-carrying gas KTEG, is selected from the one in following materials or 2 kinds or several:

1. heat-carrying gas KTEG, with flow C F01 from same organic stream F00; Logistics F00 is Coal Liquefaction reaction effluent;

Be separated organic stream F00, obtain heat-carrying gas KTEG and flow C F01;

2. heat-carrying gas KTEG, finally as the feed stream FTOAFU of process AFU; Process AFU is the deep hydrogenation grading process of Coal Liquefaction process gained Coal Liquefaction oil;

Hydrocarbon ils HPF-TOAFU enters process AFU;

3. heat-carrying gas KTEG is the feed stream FTOAFU of process AFU; Process AFU is the deep hydrogenation grading process of Coal Liquefaction process gained Coal Liquefaction oil;

Hydrocarbon ils HPF-TOAFU enters process AFU;

4. heat-carrying gas KTEG is the feed stream FTOAFU of process AFU; Process AFU is the deep hydrogenation grading process of Coal Liquefaction process gained Coal Liquefaction oil;

Hydrocarbon ils HPF-TOAFU enters process AFU;

5. heat-carrying gas KTEG, enters associating course of processing AFSH after mixing with the hydrocarbon component based on flow C F01; AFSH is deep hydrogenation grading process;

Hydrocarbon ils HPF-TOAFU enters associating course of processing AFSH;

6. heat-carrying gas KTEG, enters associating course of processing AFSH after mixing with the hydrocarbon component based on flow C F01; AFSH is the liquefied coal coil Hydrogenation available hydrogen oil process preparing hydrogen supply agent;

Hydrocarbon ils HPF-TOAFU enters associating course of processing AFSH;

7. heat-carrying gas KTEG, enters Coal Liquefaction process R10 after mixing serve as solvent oil with the hydrocarbon component based on flow C F01; Heat-carrying gas KTEG is from liquefied coal coil Hydrogenation available hydrogen oil process gained hydrogen supply dissolvent oil or hydrogen supply dissolvent oil distillate oil;

Hydrocarbon ils HPF-TOR10 is obtained at recycling step S2, separated stream S1V; Hydrocarbon ils HPF-TOR10 contains the most of conventional liquid hydrocarbon in heat-carrying gas KTEG and the close component of boiling point from flow C F01;

Hydrocarbon ils HPF-TOR10 enters Coal Liquefaction process R10;

8. heat-carrying gas KTEG is the hydrocarbon ils HPF-RP that recycling step S2 separated stream S1V obtains;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

Hydrocarbon ils HPF-RP absorbs after heat through heat-processed HX01 and is converted into hot logistics HPF-RP-E at least partially, and hot logistics HPF-RP-E recycles as heat-carrying gas KTEG at least partially;

The present invention, at the first vaporization separate part S1, containing coalite tar in solid particulate or its distillate or its hot procedure or its hydrogenation process gained oil product; Described hot procedure comprises coking, catalytic cracking process, catalytic pyrolysis process, visbreaking process, thermal cracking process; Described hydrogenation process comprises unifining process, hydrocracking process, heat from hydrogenation cracking process, hydro-upgrading process; Usually, heat-carrying gas KTEG, is selected from the one in following materials or 2 kinds or several:

1. heat-carrying gas KTEG, with flow C F01 from same organic stream F00; Logistics F00 is the middle coalite tar containing solid particulate;

Be separated organic stream F00, obtain heat-carrying gas KTEG and flow C F01;

2. heat-carrying gas KTEG, finally as the feed stream FTOAFU of process AFU; Process AFU is the deep hydrofinishing process of hydrocarbon ils HPF-TOAFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

3. heat-carrying gas KTEG, finally as the feed stream FTOAFU of process AFU; Process AFU is the deep hydrofinishing process of hydrocarbon ils HPF-TOAFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

4. heat-carrying gas KTEG, finally as the feed stream FTOAFU of process AFU; Process AFU is the deep hydrofinishing process of hydrocarbon ils HPF-TOAFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

5. heat-carrying gas KTEG, finally as the feed stream FTOAFU of process AFU; Process AFU is the deep hydrofinishing process of hydrocarbon ils HPF-TOAFU;

Hydrocarbon ils HPF-TOAFU is obtained at recycling step S2, separated stream S1V; Hydrocarbon ils HPF-TOAFU contains the conventional liquid hydrocarbon of more than 98% in heat-carrying gas KTEG;

Hydrocarbon ils HPF-TOAFU enters process AFU;

6. heat-carrying gas KTEG is the hydrocarbon ils HPF-RP that recycling step S2 separated stream S1V obtains;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

The present invention usually, is vacuum distillation process in the process of recycling step S2, separated stream S1V.

The present invention, the first vaporization separate part S1, at least can comprise 3 serial operation steps of flow C F01: pneumatic dispersion steps S1DS, gas heating step S1RT and flash separation step S1F;

At pneumatic dispersion steps S1DS, gas stream S1V does work as disperse power gas percussion flow C F01, contained by flow C F01, solid particulate realizes discretize at least partially, thus increases the exterior surface area of the total solids particle of logistics CF01, obtains pneumatic dispersion steps S1DS effluent S101P;

At gas heating step S1RT, gas stream S1V, as heated gas heats discretize flow C F01, obtains gas heating step S1RT effluent S102P;

At flash separation step S1F, effluent S102P is separated into and may contains the gas stream S1V of solid and the logistics S1SL at least containing solid particulate;

Usually, at pneumatic dispersion steps S1DS, gas stream S1V does work as disperse power gas percussion flow C F01, and contained by most of flow C F01, solid particulate realizes discretize, thus increase the exterior surface area of the total solids particle of logistics CF01, obtain pneumatic dispersion steps S1DS effluent S101P;

Usually, at gas heating step S1RT, gas stream S1V, as heated gas heats discretize flow C F01, obtains gas heating step S1RT effluent S102P;

Usually, at flash separation step S1F, effluent S102P is separated into gas stream S1V containing solid and containing solid particulate, logistics S1SL containing heavy hydrocarbon.

The present invention, the first vaporization separate part S1, at least can comprise 4 series connection steps of flow C F01: operate pneumatic dispersion steps S1DS, gas heating step S1RT, depressurization step S1DP and flash separation step S1F;

At depressurization step S1DP, effluent S102P decompression becomes depressurization step S1DP effluent S103P;

Usually, at depressurization step S1DP, effluent S102P decompression becomes depressurization step S1DP effluent S103P;

The present invention, the first vaporization separate part S1, at least comprises 3 series connection steps of flow C F01: operate pneumatic dispersion steps S1DS, gas heating step S1RT and flash separation step S1F;

Flash separation step S1F working pressure: be usually less than 0.17MPaA, be generally preferably lower than 0.05MPaA lower than 0.10MPaA.

Gas heating step S1RT working pressure: usually above 0.10MPaA, be generally 0.15 ~ 0.50MPaA, preferably is 0.15 ~ 0.30MPaA, be preferably 0.20 ~ 0.30MPaA.

The present invention, the first vaporization separate part S1, can comprise 2 or multiple pneumatic dispersion steps S1DSX.

The present invention, the first vaporization separate part S1, can comprise 2 or multiple gas heating step S1RTX.

The present invention, the first vaporization separate part S1, can comprise 2 or multiple depressurization step S1DPX.

The present invention, the first vaporization separate part S1, can comprise 2 or multiple flash separation step S1FX.

The present invention, first vaporization separate part S1,2 or multiple pneumatic dispersion steps S1DS, 2 or multiple gas heating step S1RT, 2 or multiple depressurization step S1DP, 2 or multiple flash separation step S1F can be comprised, above-mentioned steps is series relationship, and its series system is selected from mathematical syntagmatic.

The present invention, usually, heat-carrying gas KTEG is the hydrocarbon composition of 160 ~ 410 DEG C or 160 ~ 250 DEG C or 250 ~ 410 DEG C primarily of normal boiling point.

Embodiment

Below describe the present invention in detail.

Pressure of the present invention, refers to absolute pressure.

Concentration of component of the present invention, when not specializing, is weight concentration and mass concentration.

Conventional gas hydrocarbon of the present invention is the hydro carbons of gaseous state under referring to normal condition, comprises methane, ethane, propane, butane; The hydro carbons be in a liquid state under conventional liq hydrocarbon of the present invention refers to normal condition, comprises pentane and the higher hydro carbons of boiling point thereof; Impurity composition of the present invention refers to the hydrocracking thing of non-hydrocarbon component in stock oil as water, ammonia, hydrogen sulfide, hydrogenchloride etc.

In order to describe the problem, coalite tar heavy oil in routine or residual oil or the coal-tar pitch coal tar fraction of 500 DEG C (the such as normal boiling point higher than) are divided into light residue fraction and heavy resid component to treat by the present invention, are such as that the coal tar component of 500 ~ 540 DEG C is called the light residue fraction of coal tar, normal boiling point is called coal tar heavy duty residue fraction higher than the coal tar component of 540 DEG C by normal boiling point.Light residue fraction of the present invention and heavy resid component are a kind of concepts relatively.

Coal-based oil of the present invention, refers to the hydrocarbon ils from coal charge that the dry distillation of coal or coking of coal or the coal hot procedure such as coal generating gas or the direct liquefaction of coal hydrogenation produce, comprises semi coking tar, middle temperature tar, high temperature tar, liquefied coal coil and mixing oil thereof.

Coal-based heavy oil of the present invention, refer to and compare as generally described from the coal-tar pitch of coal tar primarily of the cut of normal boiling point higher than the coal-based oil ingredient composition of 500 DEG C, usually contain a large amount of macromolecular substance as polycyclic aromatic hydrocarbons, colloid, bituminous matter etc., its hydrogen richness is lower, ash oontent is higher.

Coal-based heavy oil component of the present invention, refers to normal boiling point in coal-based oil higher than the hydrocarbon ils component of 500 DEG C, usually containing a large amount of macromolecular substance as polycyclic aromatic hydrocarbons, colloid, bituminous matter etc., its hydrogen richness is lower.

Coal tar of the present invention, refer to the coal tar from the process such as pyrolysis step of pyrolysis of coal or coking of coal or the dry distillation of coal or coal generating gas process or its cut, can be by product coalite tar or its cut of coal generating gas, also can be coal coking pyrolysis of coal process (comprising semi-coking, middle temperature coking, high-temperature coking process) by product coal tar or its cut, coal tar of the present invention can also be the mixing oil of above-mentioned coal tar.Coal tar of the present invention, comprises semi coking tar, middle temperature tar, high temperature tar, the mixing oil of different coal tar, the distillate of coal tar.

High-temperature coking belongs to coal high temperature pyrolysis process, and the outlet temperature of pyrolytic process is generally greater than 900 DEG C, usually between 1000 ~ 1400 DEG C.Described coal-tar heavy oil refers to the by product crude tar oil that coal high temperature pyrolysis produces coke and/or the production of town gas process.Coal-tar heavy oil is in primary distillation process, the following product of usual production: the products such as light oil (topping tar), carbolic oil, naphtalene oil, lightweight washing oil, heavy wash oil, lightweight carbolineum, heavy carbolineum, pitch, carbolic oil can be separated into crude phenols and dephenolize oil further, and naphtalene oil can be separated into thick naphthalene and de-naphtalene oil further.Coal-tar heavy oil lighting end of the present invention refers to: carbolineum, washing oil, naphtalene oil, de-naphtalene oil, carbolic oil, dephenolize oil, light oil and mixing oil thereof.

Because raw coal character and coking or gas-making process condition change all within the specific limits, coal tar oil properties also changes within the specific limits.Processing condition and the product requirement of coal tar primary distillation process also change within the specific limits, therefore the character of coal tar lighting end also changes within the specific limits.The character of coal tar lighting end, proportion is generally 0.92 ~ 1.25, normal boiling point is generally 60 ~ 500 DEG C and is generally 120 ~ 460 DEG C, usual metal content is 5 ~ 80PPm, sulphur content is 0.4 ~ 0.8%, nitrogen content is 0.6 ~ 1.4%, oxygen level is 0.4 ~ 9.0%, usual water-content is 0.2 ~ 5.0%, and carbon residue content is generally 0.5 ~ 13%.

The normal boiling point of middle coalite tar comprises coal-tar pitch higher than the last running of 350 DEG C, and its suitable method of hydrotreating is the heat from hydrogenation cracking process using upflowing expanded bed, and following process can supporting hydro-upgrading process as required; Beds mode of operation upflowing expanded bed, can be selected from following in a kind or several combinations:

1. suspension bed and slurry bed system;

2. ebullated bed;

3. upflowing moving-bed;

4. upflowing slight expanded-bed.

DCL/Direct coal liquefaction process of the present invention, refers to the method being made gelatin liquefaction under solvent oil exists by hydrogenation, according to the difference of solvent oil and catalyzer, pyrolysis way and the difference of hydrogenation mode and the difference of processing condition, can be divided into following several technique:

1. pyrolysis liquefaction process is dissolved: utilize heavy solvent can obtain low-ash extract (Japan claims swelling charcoal) to pyrolysis of coal extracting; Utilize light solvent at supercritical conditions extracting can obtain the oils based on mink cell focus.This method is without hydrogen, though the high product of front a kind of process yield is still solid, rear a kind of technique is as not too high in supercritical extraction (extraction) method (SCE) extract content;

2. solvent hydrogenation extracting liquefaction process: if any solvent refined coal process 1 and II (SRC-1 and SRC-II), Exxon donor solvent process EDS, Japanese New Energy Development Organization liquefaction process (NEDOL) etc., use hydrogen, but pressure is not too high, solvent oil has obvious effect;

3. Hydrogenation method: as the old and new's liquefaction process (IG and NewlG) of Germany and the H-coal process (H-Coal) etc. of the U.S. all belong to this class;

4. coal and residual oil associating processing method (COprocessing): be that solvent oil once passes through reactor, without turning oil together with coal with residual oil.There is hydrocracking simultaneously and be converted into lightweight oil in residual oil.The technique that the U.S., Canada, Germany and USSR (Union of Soviet Socialist Republics) etc. are had nothing in common with each other;

5. destructive distillation liquefaction process: the first pyrolysis of coal obtains tar, then carries out hydrocracking and upgrading to tar;

6. underground liquefaction process: solvent is injected subterranean coal, makes coal depolymerization and dissolving, adds that the surging force of fluid makes coal collapse loose, and not consoluet coal is then suspended in solvent, to be extracted out by solution and be separated processing with pump.

In coal direct liquefaction method, majority belongs to direct hydrogenation liquefaction of coal liquefaction process, no matter which kind of coal faces hydrogen direct liquefaction process, its target is all obtain oil product, and the function of pursuit is all " coal turns oil ", and the chemical transformation that must exist is " coal hydrogenation ", the common trait of this type of technology uses solvent oil and catalyzer at present, the conventional boiling range of solvent oil is generally 200 ~ 450 DEG C, majority is 200 ~ 400 DEG C, and solvent oil majority is distilled oil, and contained aromatic hydrocarbons majority is the aromatic hydrocarbons of 2 ~ 4 ring structures.Therefore, no matter be which kind of coal faces hydrogen direct liquefaction process, the outer oil extraction that its produces or liquefied coal coil (being generally gelatin liquefaction light oil) or liquefied coal coil modified oil, as long as its composition possesses raw material compositing characteristic of the present invention, all can use the inventive method to process.

The thermally dissolving and catalytic of a kind of brown coal preparing liquid fuel that patent CN100547055C states clearly is owned by France in brown coal medium-pressure hydrocracking direct liquefaction process, comprises Coal liquefaction process and liquefied coal coil hydrogenation modification process totally two processes.In order to improve the transformation efficiency of coal direct liquefaction and realize coal feedstock and enter reactor, coal makes coal dust before entering reactor usually, be made into coal oil mixture with the solvent oil possessing good hydrogen supply capacity, coal oil mixture enters reactor after pressurization, heating.

Coal liquefaction process of the present invention, refer to coal and the molecule hydrogen that may exist as raw material, with specific oil product (being generally the hydrogenation modification oil of liquefied coal coil) for hydrogen supply dissolvent oil, under certain operational condition (as service temperature, working pressure, solvent oil/coal weight ratio, hydrogen/solvent oil volume ratio and suitable hydrogenation catalyst), directly there is the reaction process of carbon-carbon bond thermally splitting, hydrogenation liquefaction in coal.

Liquefied coal coil of the present invention, refer to the oil product that described Coal liquefaction process produces, it is present in Coal Liquefaction reaction effluent, is to consume coal based on hydrogen supply dissolvent oil, reaction and react the combined reaction product of transfer hydrogen.

After Coal liquefaction process works well, hydrogen supply dissolvent oil usually adopts the hydrogenation modification oil of the self-produced liquefied coal coil of Coal liquefaction process (being generally conventional boiling range higher than the distillate of 165 DEG C), the major objective of liquefied coal coil hydrogenation modification process produces Coal liquefaction process solvent oil, be exactly specifically the content improving " there is the component of good hydrogen supply function " in oil product, such as improve cycloalkyl benzene class, the content of bicyclic alkyl benzene class component, a large amount of double ring arene and this fact of a large amount of thrcylic aromatic hydrocarbon is contained based on liquefied coal coil, liquefied coal coil hydrogenation modification process is the hydrogenation process of " appropriate aromatic saturation ".

The ultimate aim of Coal liquefaction process produces the oil product of outer confession, the hydrogenation modification oil content that usual liquefied coal coil hydrogenation modification process produces is two portions: a part is used as Coal liquefaction process hydrogen supply dissolvent oil, and a part is used as the outer oil extraction of gelatin liquefaction liquefaction process.Usually, the light oil of gelatin liquefaction at least partially that Coal liquefaction process produces is used as the outer oil extraction A of coal liquifaction process, remaining liquefied coal coil is used as liquefied coal coil hydrogenation modification process stock oil and produces Coal liquefaction process hydrogen supply dissolvent oil and outer oil extraction B, now there is the outer oil extraction of A and B two-way, the final whereabouts of the outer oil extraction of A and B two-way is all through deep hydrogenation grading process production high-quality oil product such as diesel oil distillate, naphtha fraction usually.

The method of a kind of oil-containing porous carbon of the present invention solids extract oil, is characterized in that comprising following steps:

1. logistics HPF9S mixes with logistics S1SL;

2. logistics HPF9S contacts with heat-carrying gas KTEG;

3. logistics HPF9S contacts with flow C F01.

1. direct hydrogenation liquefaction of coal process gained semicoke particle;

2. granules of catalyst;

3. iron rust particle;

4. particles of inorganic material;

7. from the solid particulate of shale;

8. from the solid particulate of oil-sand;

9. other is present in the particle in flow C F01.

1. heat-carrying gas KTEG, with flow C F01 from same logistics F00;

Be separated organic stream F00, obtain heat-carrying gas KTEG and flow C F01;

1. heat-carrying gas KTEG, the logistics F00 produced from same hydrogenation process R10 with flow C F01;

Separated stream F00, obtains heat-carrying gas KTEG and flow C F01;

3. heat-carrying gas KTEG, finally as the feed stream FTOAFU of process AFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

4. heat-carrying gas KTEG is the feed stream FTOAFU of process AFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

5. heat-carrying gas KTEG is the feed stream FTOAFU of process AFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

Hydrocarbon ils HPF-TOAFU enters associating course of processing AFSH;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

Be separated organic stream F00, obtain heat-carrying gas KTEG and flow C F01;

Hydrocarbon ils HPF-TOAFU enters process AFU;

Hydrocarbon ils HPF-TOAFU enters associating course of processing AFSH;

Hydrocarbon ils HPF-TOR10 enters Coal Liquefaction process R10;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

The present invention, at the first vaporization separate part S1, containing coalite tar in solid particulate or its distillate or its hot procedure or its hydrogenation process gained oil product; Described hot procedure comprises coking, catalytic cracking process, catalytic pyrolysis process, visbreaking process, thermal cracking process; Described hydrogenation process comprises unifining process, hydrocracking process, heat from hydrogenation cracking process, hydro-upgrading process;

Usually, heat-carrying gas KTEG, is selected from the one in following materials or 2 kinds or several:

Be separated organic stream F00, obtain heat-carrying gas KTEG and flow C F01;

Hydrocarbon ils HPF-TOAFU enters process AFU;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

Claims

1. extract a method for oil in the logistics of self-contained solid particulate and heavy hydrocarbon, it is characterized in that comprising following steps:

2. method according to claim 1, is characterized in that:

3. method according to claim 1, is characterized in that:

(1) 50% of conventional liquid hydrocarbon distillate a normal boiling point temperature CF01-NBP50 in flow C F01, deduct 50% of conventional liquid hydrocarbon in heat-carrying gas KTEG and distillate a normal boiling point temperature KTE6-NBP50 gained temperature gap DT1 and be greater than 100 DEG C;

4. method according to claim 1, is characterized in that:

5. method according to claim 1, is characterized in that:

(2) different hydrocarbon stream HPF1 and HPF2 of at least two boiling ranges is obtained at recycling step S2, separated stream S1V;

6. method according to claim 1, is characterized in that:

(2) the hydrocarbon liquid phase logistics HPF9S containing solid is obtained at recycling step S2, separated stream S1V.

7. method according to claim 1, is characterized in that:

(2) the hydrocarbon liquid phase logistics HPF9S containing solid is obtained at recycling step S2, separated stream S1V;

Logistics HPF9S mixes with logistics S1SL.

8. method according to claim 1, is characterized in that:

Logistics HPF9S contacts with heat-carrying gas KTEG.

9. method according to claim 1, is characterized in that:

Logistics HPF9S contacts with flow C F01.

10. method according to claim 1, is characterized in that:

Logistics HPF9S with return the first vaporization separate part S1 and contact with process stream, the vaporization of hydro carbons at least partially in logistics HPF9S enters in gas S1V.

11. methods according to claim 1, is characterized in that:

(1) at the first vaporization separate part S1, the most of normal boiling point in flow C F01 enters in gas S1V lower than the hydro carbons vaporization of 480 DEG C.

12. methods according to claim 1, is characterized in that:

(1) at the first vaporization separate part S1, the most of normal boiling point in flow C F01 enters in gas S1V lower than the hydro carbons vaporization of 500 DEG C.

13. methods according to claim 1, is characterized in that:

(1) at the first vaporization separate part S1, the most of normal boiling point in flow C F01 enters in gas S1V lower than the hydro carbons vaporization of 520 DEG C.

14. methods according to claim 1, is characterized in that:

(1) at the first vaporization separate part S1, the most of normal boiling point in flow C F01 enters in gas S1V lower than the hydro carbons vaporization of 540 DEG C.

15. methods according to claim 1, is characterized in that:

(1) at the first vaporization separate part S1, the most of normal boiling point in flow C F01 enters in gas S1V lower than the hydro carbons vaporization of 555 DEG C.

16. methods according to claim 1, is characterized in that:

(1) be that the part by weight defining the conventional liquid hydrocarbon in logistics S1SL is K99, K99≤0.50 containing solid, logistics containing conventional liquid hydrocarbon at the first vaporization separate part S1, logistics S1SL.

17. methods according to claim 16, is characterized in that:

(1) at the first vaporization separate part S1, K99≤0.40.

18. methods according to claim 16, is characterized in that:

(1) at the first vaporization separate part S1, K99≤0.30.

19. methods according to claim 16, is characterized in that:

(1) at the first vaporization separate part S1, K99≤0.20.

20. methods according to claim 16, is characterized in that:

(1) at the first vaporization separate part S1, K99≤0.10.

21. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 or 18 or 19 or 20, is characterized in that:

Containing the flow C F01 of solid particulate and heavy hydrocarbon, be selected from the one in following materials or 2 kinds or several:

22. methods according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 or 18 or 19 or 20, is characterized in that:

Containing the flow C F01 of solid particulate and heavy hydrocarbon, described solid particulate be selected from following in one or 2 kinds or several:

1. direct hydrogenation liquefaction of coal process gained semicoke particle;

2. granules of catalyst;

3. iron rust particle;

4. particles of inorganic material;

7. from the solid particulate of shale;

8. from the solid particulate of oil-sand;

9. other is present in the particle in flow C F01.

23. methods according to claim 21, is characterized in that:

(1) at the first vaporization separate part S1, the gross weight WRC-KTEG of the conventional liquid hydrocarbon in heat-carrying gas KTEG is defined as KWW divided by the gross weight WRC-CF01 of the conventional liquid hydrocarbon in flow C F01, namely KWW=(WRC-KTEG)/(WRC-CF01), KWW are 0.01 ~ 100.

24. methods according to claim 23, KWW is 1.0 ~ 20.

25. methods according to claim 21, is characterized in that:

(1) at the first vaporization separate part S1, the gross weight WRC-KTEG of the conventional liquid hydrocarbon in heat-carrying gas KTEG is defined as KWT divided by the gross weight WT-CF01 of flow C F01, namely KWT=(WRC-KTEG)/(WT-CF01), KWT are 0.01 ~ 40.

26. methods according to claim 25, KWT is 2.0 ~ 5.

27. methods according to claim 21, is characterized in that:

(1) at the first vaporization separate part S1, containing the flow C F01 of solid particulate and heavy hydrocarbon, for containing the direct hydrogenation liquefaction of coal process gained direct hydrogenation liquefaction of coal oil of solid particulate or its distillate or its hot procedure gained oil product;

28. methods according to claim 27, is characterized in that:

(1) at the first vaporization separate part S1, containing the flow C F01 of solid particulate and heavy hydrocarbon, for containing the direct hydrogenation liquefaction of coal process gained Coal Liquefaction oil of solid particulate or its distillate or its hot procedure gained oil product;

29. methods according to claim 21, is characterized in that:

Heat-carrying gas KTEG, is selected from the one in following materials or 2 kinds or several:

1. heat-carrying gas KTEG, with flow C F01 from same logistics FOO;

Be separated organic stream FOO, obtain heat-carrying gas KTEG and flow C F01;

2. heat-carrying gas KTEG, the logistics FOO produced from same hydrogenation process R10 with flow C F01;

Separated stream FOO, obtains heat-carrying gas KTEG and flow C F01;

3. heat-carrying gas KTEG, finally as the feed stream FTOAFU of process AFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

4. heat-carrying gas KTEG is the feed stream FTOAFU of process AFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

5. heat-carrying gas KTEG is the feed stream FTOAFU of process AFU;

Hydrocarbon ils HPF-TOAFU enters process AFU;

Hydrocarbon ils HPF-TOAFU enters associating course of processing AFSH;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

30. methods according to claim 21, is characterized in that:

(1) at the first vaporization separate part S1, containing the flow C F01 of solid particulate and heavy hydrocarbon, for containing the Coal Liquefaction process R10 gained Coal Liquefaction oil of solid particulate or its distillate;

1. heat-carrying gas KTEG, with flow C F01 from same organic stream FOO; Logistics FOO is Coal Liquefaction reaction effluent;

Be separated organic stream FOO, obtain heat-carrying gas KTEG and flow C F01;

Hydrocarbon ils HPF-TOAFU enters process AFU;

Hydrocarbon ils HPF-TOAFU enters associating course of processing AFSH;

Hydrocarbon ils HPF-TOR10 enters Coal Liquefaction process R10;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

31. methods according to claim 21, is characterized in that:

(1) at the first vaporization separate part S1, containing coalite tar in solid particulate or its distillate or its hot procedure or its hydrogenation process gained oil product; Described hot procedure comprises coking, catalytic cracking process, catalytic pyrolysis process, visbreaking process, thermal cracking process; Described hydrogenation process comprises unifining process, hydrocracking process, heat from hydrogenation cracking process, hydro-upgrading process;

1. heat-carrying gas KTEG, with flow C F01 from same organic stream FOO; Logistics FOO is the middle coalite tar containing solid particulate;

Be separated organic stream FOO, obtain heat-carrying gas KTEG and flow C F01;

Hydrocarbon ils HPF-TOAFU enters process AFU;

Hydrocarbon ils HPF-RP is obtained at recycling step S2, separated stream S1V;

32. methods according to claim 1, is characterized in that:

(2) be vacuum distillation process in the process of recycling step S2, separated stream S1V.

33. methods according to claim 21, is characterized in that:

34. methods according to claim 1, is characterized in that:

(1) first vaporization separate part S1, at least comprises 3 serial operation steps of flow C F01: pneumatic dispersion steps S1DS, gas heating step S1RT and flash separation step S1F;

At flash separation step S1F, effluent S102P is separated into may the gas stream S1V containing solid and the logistics S1SL at least containing solid particulate.

35. methods according to claim 34, is characterized in that:

At pneumatic dispersion steps S1DS, gas stream S1V does work as disperse power gas percussion flow C F01, contained by major part flow C F01, solid particulate realizes discretize, thus increases the exterior surface area of the total solids particle of logistics CF01, obtains pneumatic dispersion steps S1DS effluent S101P;

At flash separation step S1F, effluent S102P is separated into gas stream S1V containing solid and containing solid particulate, logistics S1SL containing heavy hydrocarbon.

36. methods according to claim 34, is characterized in that:

(1) first vaporization separate part S1, at least comprises 4 series connection steps of flow C F01: operate pneumatic dispersion steps S1DS, gas heating step S1RT, depressurization step S1DP and flash separation step S1F;

37. methods according to claim 35, is characterized in that:

38. methods according to claim 34, is characterized in that:

(1) first vaporization separate part S1, at least comprises 3 series connection steps of flow C F01: operate pneumatic dispersion steps S1DS, gas heating step S1RT and flash separation step S1F;

Flash separation step S1F working pressure is lower than 0.17MPaA.

39. methods according to claim 34, is characterized in that:

Flash separation step S1F working pressure is lower than 0.10MPaA.

40. methods according to claim 34, is characterized in that:

Flash separation step S1F working pressure is lower than 0.05MPaA.

41. methods according to claim 34, is characterized in that:

Gas heating step S1RT working pressure is higher than 0.10MPaA.

42. methods according to claim 34, is characterized in that:

Gas heating step S1RT working pressure is 0.15 ~ 0.50MPaA.

43. methods according to claim 34, is characterized in that:

Gas heating step S1RT working pressure is 0.15 ~ 0.30MPaA.

44. methods according to claim 34, is characterized in that:

Gas heating step S1RT working pressure is 0.20 ~ 0.30MPaA.

45. methods according to claim 1, is characterized in that:

(1) first vaporization separate part S1, comprises 2 or multiple pneumatic dispersion steps S1DSX.

46. methods according to claim 1, is characterized in that:

(1) first vaporization separate part S1, comprises 2 or multiple gas heating step S1RTX.

47. methods according to claim 1, is characterized in that:

(1) first vaporization separate part S1, comprises 2 or multiple depressurization step S1DPX.

48. methods according to claim 1, is characterized in that:

(1) first vaporization separate part S1, comprises 2 or multiple flash separation step S1FX.

49. methods according to claim 1, is characterized in that:

(1) first vaporization separate part S1, comprise 2 or multiple pneumatic dispersion steps S1DS, 2 or multiple gas heating step S1RT, 2 or multiple depressurization step S1DP, 2 or multiple flash separation step S1F, above-mentioned steps is series relationship, and its series system is selected from mathematical syntagmatic.

50. methods according to claim 1, is characterized in that:

(1) at the first vaporization separate part S1, heat-carrying gas KTEG is the hydrocarbon composition of 160 ~ 410 DEG C primarily of normal boiling point.

51. methods according to claim 1, is characterized in that:

(1) at the first vaporization separate part S1, heat-carrying gas KTEG is the hydrocarbon composition of 160 ~ 250 DEG C primarily of normal boiling point.

52. methods according to claim 1, is characterized in that:

(1) at the first vaporization separate part S1, heat-carrying gas KTEG is the hydrocarbon composition of 250 ~ 410 DEG C primarily of normal boiling point.