CN105602601A

CN105602601A - Coal-to-oil catalytic extraction technology and special device thereof

Info

Publication number: CN105602601A
Application number: CN201511017682.8A
Authority: CN
Inventors: 金先奎; 林秀惠
Original assignee: Individual
Current assignee: Individual
Priority date: 2015-12-30
Filing date: 2015-12-30
Publication date: 2016-05-25

Abstract

The invention relates to a coal-to-oil catalytic extraction technology. The technology concretely comprises the steps of firstly, pulverizing coal by a pulverizer, and enabling the pulverized coal to enter a slurry preparation tank; enabling the slurry preparation tank to stir in an intermittent way, and enabling the pulverized coal and oil to be fully mixed together to form a coal slurry state; enabling the coal slurry to enter a tubular heater; reducing the pressure of the reaction product coming out from a pure axial flow reactor, then enabling the reaction product to enter a high-pressure separating tank, and carrying out flash evaporation on the reaction product; enabling light oil constituent coming out from the top of the high-pressure separating tank to enter the bottom of a rectifying tower in the form of gas phase; enabling the reaction product at the bottom of the high-pressure separating tank to enter a low-pressure separating tank; enabling product oil to come out from the top of the rectifying tower, and enabling a solvent to come out from the bottom of the rectifying tower; cooling the product oil, then enabling the cooled product oil to enter a storage tank and enabling the solvent to enter a solvent tank for recycling. The invention also provides a special device of the coal-to-oil catalytic extraction technology. The device comprises the pulverizer, the slurry preparation tank, the heater, the reactor, the high-pressure separating tank, the low-pressure separating tank, a vacuum tank and a solvent recovery tower; all the modules are sequentially connected. The coal-to-oil catalytic extraction technology and the special device of the coal-to-oil catalytic extraction technology have the advantages that the production technology is simplified, the equipment efficiency is improved, the energy consumption of production is reduced, the pollution is reduced, the raw material utilization rate is improved, and the production cost per ton of oil is lowered.

Description

A kind of catalytic extraction coal oil-producing technique and special purpose device thereof

Technical field

The present invention relates to catalytic extraction coal liquefaction field, particularly a kind of catalytic extraction coal systemOil technique and special purpose device thereof.

Background technology

First, catalytic extraction coal liquefaction is to deviate from oxygen, sulphur, nitrogen and heavy by hydrofinishingThe thick light diesel fuel of metal. Containing aromatic hydrocarbons such as naphthalene, phenol, be the substitute of oil, coal liquefaction is as oneThe resource of planting alternative oil, country pays much attention to. Along with international, domestic petroleum imbalance between supply and demandAggravation, the paces of accelerating the technological development of coal liquefaction have become the common recognition of all circles, the product of coal liquefactionIndustry development rapidly. At present, China's oil dependence on external supply degree has reached more than 60%, energy warA little less than slightly safety is highly brittle; And rich coal resources, the reserves of having verified approximately can be exploitedMore than 2000 year is trend of the times so coal liquefaction replaces oil.

In prior art coal liquefaction Fischer-Tropsch synthetic technology and the oil product process technology supporting with it andCoal Direct Hydrogenation liquefaction process.

(1) Fischer-Tropsch synthetic (Fischer-Tropschsynthesis is called for short F-T synthetic) technology and withThe oil product process technology that it is supporting, integrated other necessary technology becomes as: coal gasification, water-gasChange, purified synthesis gas, sulfur recovery, synthetic cyclic gas decarburization, the processing of synthesis tail gas oil wash, closeBecome the main technique technology such as water treatment,

Since F-T synthetic technology refers to 1997 at Chinese Academy of Sciences's Shanxi coal chemical researchWhat synthesized oil product ERC implemented is produced through the synthetic hydro carbons of producing of F-T by synthesis gasThe complex art of product. The scope that technology contains is synthetic catalyst and its production technology, F-TSynthetic pulp state bed reactor, comprises the Design and manufacture scheme of process matching, reactor, syntheticTechnique is integrated, follows around the synthesis gas of the synthetic core catalyst of F-T and reactor technology compositionLoop back path, circulating air decarburization Integrated Solution, low temperature oil wash Integrated Solution, waste gas utilization scheme,Synthetic water processing scheme, product solution. The oil product process technology of independent intellectual property right refers to basisSynthetic technology product structure and feature, since calendar year 2001, SynfuelsChina is with domestic relevantWhat research and design department developed jointly passes through hydrofinishing, hydrogenation by F-T Synthin productA series of processing final production such as cracking LPG, naphtha (or lightnaphtha), diesel oil, liquid(catalyst, reactor and the technique) of the product such as paraffin body/raw material for alkylation, paraffin is completeTechnology.

Artificial oil technology: adoptSeries F-T synthetic catalyst,Under 240-250oC and 15-20Mpa (A) effective pressure, carry out synthetic heavy cut for mainF-T product, F-T product are main oil product process life through hydrofinishing and hydrocrackingProduce the complete synthetic oil technical side of LPG8-15%, naphtha 12-20%, diesel oil 65-80%Case. This technology also can considered other high added value chemical industry aspect product processing configurationThe production of product. Due to the F-T synthetic reaction of this process technology be carry out at a lower temperature,And produce more heavy wax product, therefore claim low temperature slurry state bed synthesis technique or heavy end to synthesizeTechnique.

Artificial oil technology: adoptSeries F-T synthetic catalyst,Under 260-270 degree Celsius and 15-20Mpa (A) effective pressure, carrying out synthetic middle distillate is divided intoMain F-T product, F-T product are that main oil product was processed through hydrofinishing and hydrocrackingJourney is produced the complete synthetic oil skill of LPG8-15%, naphtha 12-25%, diesel oil 60-80%Art scheme. This technology also can considered other high added values aspect product processing configurationThe production of chemical products. Because the F-T synthetic reaction of this process technology is to enter under higher temperatureGo and produce more lightweight F-T product, therefore claim high temperature slurry state bed synthesis technique or lightweight to heat up in a steamerDivide synthesis technique.

(2) coal Direct Hydrogenation liquefaction process summary

Generally liquefaction hydrogenation process is divided into several sections and carries out, be i.e. liquid-phase hydrogenatin section, gas phase hydrogenationSection and product purification section.

In the first stage of Coal Liquefaction process, in so-called liquid-phase hydrogenatin section, carry out cracking and addHydrogen, makes the pyrolysis of coal organic macromolecule generate the free radical fragment of medium molecule, is combined with hydrogen thereupon,Obtaining boiling point is 325～340 DEG C of following products, and synthetic crude is sometimes thick also referred to as liquefactionOil is gone back tentatively removing of aerobic, nitrogen, sulphur compound simultaneously, generates water, ammonia and hydrogen sulfide.Product below 325～340 DEG C is as the raw material of further processing gasoline and diesel oil.

Second, third stage of DCL/Direct coal liquefaction process is in gas phase and has the fixed bed of catalystIn reactor, carry out, the liquid form product in liquid-phase hydrogenatin stage is first by pre-hydrogenation plant, de-at thisDenitrogenate, the compound of oxygen and sulphur, then enter cracking reformer, finally obtain merchantable gasolineWith the diesel oil refined products that is main component.

The early stage liquefaction process of Germany is the only technique of industrial practice experience for many years that has,Various new technologies basis afterwards, therefore be necessary to be first described.

The coal paste that coal, circulating solvent are prepared together with catalyst, from pans, out edge is heatedPipeline by coal paste pump at 30.OMPa or 70.OMPa, according to the pressure type heat exchange of carrying out hydrogenationDevice, reaction tower, high-temperature separator, reactor product cooler and residue cooler form. Height press-fitsPutting size and the number of middle equipment should determine according to processed raw material.

Tubular heater is arranged on the equipment place near high-pressure installation. Make in order to reduce viscosity to passHot coefficient increases and increases flowing velocity and prevents coking, enters stokehold the hydrogen of preheating is addedRare coal paste, hydrogen by high-temperature separator gas product out in heat exchanger preheating. Then rare coal pasteWith hydrogen mixture through two heat exchangers of laying in turn, by from high-temperature separator come wide heating up in a steamerThe steam dividing and the heat of gas heat, and then enter the second segment of tube furnace. Dense coal paste is straightPick the first paragraph of tube furnace; Dense coal paste is by first paragraph, mixed mutually with preheating hydrogen and rare coal pasteClose, temperature be coal paste one admixture of gas of 450 DEG C from tube furnace out, successively by lower andShangdi is by reaction tower, and the time of staying total in reaction unit is about 1h.

Hydrogenation liquefaction process is carried out in the reaction tower at 470～480 degrees Celsius of temperature, and firstIn reaction tower, hydrogenation liquefaction reaction liberated heat is for heating the coal paste and the hydrogen that initially enterMixture. Because heat is emitted in liquefaction when hydrogenation, so for fear of at Ta Nei and transfer pipelineMiddle coking, the temperature of liquefaction reaction tower can be used by 6 cold hydrogen of infeed circulation and control. This 6 pointPosition approximately equidistantly distribute by tower height degree.

The consumption of cold hydrogen of circulating is decided by raw materials used character and catalyst activity, generally existsBetween 25000～35000m3/h scope. In the total consumption of the hydrogen of sending into, the first reaction towerAccount for 30%, the second reaction tower account for 20%, the three reaction tower account for 15%, the four reactionTower accounts for 150, and high-temperature separator accounts for 20%. Dividing potential drop at stagnation pressure 70.0MPa and hydrogen isThe total pressure drop of the device operating under 65.0MPa is about 3.OMPa, the pressure of each equipmentIt is as follows that approximate range falls:

1.0MPa in heat exchanger

0.5MPa in tube furnace

0.5MPa in reaction tower and high-temperature separator

0.6MPa in heat exchanger

0.4MPa in cooler

Product and the unreacted coal etc. of liquid-phase hydrogenatin enters height from last reaction towerTemperature separator. In high-temperature separator, the gentle body of the steam of product divides with residue and separates.The mixture that residue is made up of higher boiling oil, catalyst, ash content and unconverted coal. ProductThe gentle body of steam divides by 3 heat exchangers, is cooled to 140～160 DEG C, and has part coldSolidifying, then enter high-voltage product cooler 11, be cooled to 40～50 DEG C at this.

The product of condensation together with circulating air from reactor product cooler out, enter product(cooling) separator, gas and fluid separation applications in separator. Liquid hydrogenation products subtracts specialThe step-down of pressure valve secondary, drops to 20～30MP and from 2.0～3.OMPa from 70.0MPaDrop to 0.1MPa, to reduce the speed of outflow. Now be dissolved in gas in liquid in centreIn tank, separate, and send to oil wash or further processing; The liquid product job shop of making a gift to someoneIn rectifier unit. This rectifier unit is identical with the rectifier unit in petroleum refinery, is changed by shell-and-tubeThe system of hot device, tube furnace and rectifying column forms.

In product separator, isolated gas enters in the high pressure scrubber of filling insertion ring,In scrubbing tower, from add hydrogen, wash away carburet hydrogen with flushing oil.

Residue is out sent into heat exchanger from high-temperature gas separator. In heat exchanger, residue addsThe a part of circulating air of heat, then sends into bushing type residue cooler. Cooling rear residue flows into band coneIn the closed container of shape bottom, and with special pressure-reducing valve tentatively from 70.0MPa drop to 2.0～3.0MPa, and then drop to 0.1MPa, entering the steam-heated residue tank of people, residue is sent toFurther processing is to reclaim the product liquid of carrying secretly.

Residue after dilution is sent into set from blending tank with special residue pump or residue centrifugal pumpManage and be distributed to each residue centrifuge, centrifuge operates under about 0.1MPa. By centrifugalThe oil that separation obtains enters tank, can be used for preparing coal paste and from the filter residue tank with mixer outResidue, deliver to rotary furnace low temperature distillation by pump through circulation line.

The vapour-gas mixture forming when low temperature distillation is by the deduster of oily drip washing, and entersEnter pre-cooled tower. The part condensed oil coming from tank can be used as the drip washing oil of tower, and unnecessary oil mixesAs solvent naphtha. Water-oil separating is carried out at the end. In product, contain phenol, therefore one of water layerBe distributed into cooler and make drip washing water, unnecessary water enters phenol water system to process and divideGo out commodity phenol. Oil is pumped out, after mixing, sends to rectifying with the liquid product of hydrogenation.

Pure circulating air is from inhaling people's concetrated pipe out, through opening and closing section door valve and closing soon section door valve and distributeTo each gas circulator, then enter the circulatory system. In circulating air, the average content of hydrogen is about85％。

Be provided with splash separator at the import and export of each circulating pump, splash separator is furnished with controlGather the indicator of liquid levels, in device, liquid is by manually emitting by pressure-reducing valve. At the gas of pumpBody exit liquid drop separator be below provided with cooler, can ensure gas in the system of enteringTemperature is no more than 55 DEG C.

Circulating air is divided into two plumes: one is sent to after mixing by cooler and supplementary new hydrogenMix with coal paste; Another thigh is sent to cooling reaction tower and high-temperature separator.

Send to the shell side that the circulating air mixing with coal paste enters the first high pressure heat exchanger, thereinHeated by high-temperature separator steam one liquid reacting product out, however with enter tube furnaceRare coal paste of two sections mixes.

Circulating air in high-temperature separator except cooling effect, also ensure residue stirring andWith the saturated liquid-phase hydrogenatin product of hydrogen, this has just slowed down the coking process of liquefied residue.

After high-temperature separator, circulating air enters heat exchange together with product steam-gasIn the tube side of device, then enter the new hydrogen heat exchanger of high pressure, and continue to enter by HP coolerProduct separator. In product separator, gas separates with condensing liquid product, then passes throughTentatively cooling in middle HP cooler, and after liquid drop separator, gas enters high pressureScrubbing tower, removes a large amount of impurity at this, then enters again gas circulator by separatorCirculation.

Like this, gas continuously circulates in system, and entering before hyperbaric chamber with newFresh industrial hydrogen supplements, supplement new hydrogen for the consumption of hydrogen in compensation hydrogenation process,The leakage being dissolved in hydrogen and the system in raw material is completely necessary.

In washing system, keep having in circulating air by the method for getting rid of gaseous state hydrogenation productsNecessary hydrogen content and the dividing potential drop of hydrogen.

On the transfer pipeline of the circulatory system, especially this from hyperbaric chamber to washing facilityDuan Shang, uses heat-insulation layer to reduce heat loss. Because in lower temperature, Celsius lower than 35Degree, owing to having ammonia, carbon dioxide to exist in gas, has ammonium salt precipitation in pipe, also produce simultaneouslyThe crystalline compounds of gaseous hydrocarbons and water, deposited salt and hyrate can cause the circulatory systemObstruction, easily cause production accident. Because depending primarily on, the normal operation of whole hydrogenation section followsWhether loop systems can operate without interruption, therefore the gas that general installation has very large reserve capabillity followsRing pump, and at least should have two stand-by pumps in the time of operation, wherein should there is one to start at any time.

Get back in the circulating air of the circulatory system and contain a large amount of gaseous state hydrogenation products---gaseous hydrocarbon,Therefore recyclegas will be removed gaseous hydrocarbon by oil wash in high pressure scrubber. Circulating air is enteringEnter before oil wash system, be cooled to 35 degrees Celsius through cooler I, by liquid drop separator,Then enter scrubbing tower. From high pressure scrubber, the energy of flushing oil out returns at decompressorReceive. Used oil is depressured to 3.5～3.8MPa at cylinder tank after decompressor. From this tankIn the lean gas that separates deliver to the gas holder of lean gas net so that further processing; And oil decompression is arrivedAfter 0.1MPa, enter filling and therefrom separate rich gas, then oil is made a gift to someone, and further expeling is oily again for plate columnMiddle gas, rich gas further processing obtains gaseous hydrocarbon products. In order to improve gas separation efficiency,Plate column is under reduced pressure operation sometimes. The operation of scrubbing tower is to wash forward and backward gas by measurementDensity control. Normal density difference is 0.05～0.16kg/m3.

In sum, existing coal liquefaction technology has following defect:

Fischer-Tropsch synthetic technology and the oil product process technology supporting with it:

(1) Fischer-Tropsch synthetic technology and the oil product process technology technological process supporting with it are long, auxiliaryHelp auxiliary facility many; (2) discharge exceedes 5 tons of carbon dioxide/ton oil, and air pollution is serious; (3)Resource utilization is low; (4) energy consumption is high; (5) equipment is huge, material costliness, and system complex,Invest high; (6) water consumption is large.

Coal Direct Hydrogenation liquefaction process technology:

(1) technical matters long flow path, auxiliary auxiliary facility are many, equipment component serious wear; (2)Equipment is huge, material costliness, and system complex, invests high (3) water consumption large; (4) becomeProduct oil cost is high; (5) product oil yield is lower slightly; (6) deficiency in economic performance.

Summary of the invention

The object of the invention is in order to solve problems of the prior art, spy provides oneCatalytic extraction coal oil-producing technique and special purpose device thereof.

The invention provides a kind of catalytic extraction coal oil-producing technique, it is characterized in that: described urgesChange extraction coal oil-producing technique, concrete steps are:

First, with flour mill by coal pulverizer to 180～220 order. Coal fully dissolves in solvent,By pressed powder form to coal solution form. Coal dust is delivered to coal dust by the mode that adopts gas to carryTank. Coal dust enters pulping tank from coal dust pot bottom. Pulping tank intermittent stirring formula, makes coal dust and oilFully be mixed into coal slurry state. Coal slurry enters tube heater. Heater outlet temperature reaches450 DEG C～500 DEG C, pressure is 5～10MPA. Coal dust dissolves completely in solvent, and starts to send outRaw pyrolytic reaction. Coal slurry enters pure axial flow reactor becomes coal solution. Coal solution remains on 450DEG C～500 DEG C, pressure are 5～10MPA. The time of staying of coal dust in pure axial flow reactor is 1Individual hour. 450 DEG C～500 DEG C be coal under catalyst action, there is the low-temperature space of pyrolytic reaction,Only limit to large molecular chain rupture, tall bond fission; There is not hydrogen migration phenomenon. Coal gas is coalThe product of deep decomposition, does not produce coal gas.

Industrial, temperature, heated time are all to control the important means that oil product decomposes the degree of depth.For example ethane cracking furnace decomposes the degree of depth with heated time control oil product, before boiler tube noncokingPut, to greatest extent high output of ethylene.

Enter the flash distillation of high pressure knockout drum from the reaction product decompression out of pure axial flow reactor. HighPress knockout drum top light oil constituents secondary out to reduce pressure, enter rectifier bottoms with gas phase. HighThe reaction product of pressing knockout drum bottom, goes low pressure separation pot.

The pure axial flow reactor of suspension bed is the tubular structure that employing draw ratio is greater than 1000:1, inPut ultra low dropout static mixer; Have from agitating function, prevent precipitation.

Adopt heater indirect, can utilize the method that increases heating surface (area) (HS, reduce heatingIntensity; Solve the coking problem in heating process.

Reaction product is secondary flash distillation in low pressure separation pot, and the absolute pressure of low pressure separation pot onlyFor 1Kpa. Out heavy oil component of low pressure separation pot top, enters condenser. Condensed changeBecome liquid, flow into vacuum tank. It is coal semicoke that low pressure separation pot bottom does not have the material of gasification, coalSemicoke, after being pumped to cooler, removes coal semicoke storage pool.

The heavy oil component of vacuum tank bottom goes to rectifying column middle part through pump, and vacuum tank top connects vacuumPump. By vavuum pump intrasystem on-condensible gas extract out, emptying. What vavuum pump was extracted out is emptyGas, water vapour.

Enter rectifying column middle part heavy oil component and enter rectifier bottoms light oil constituents and carry out stripping,Rectifying column top out be product oil, rectifier bottoms out be solvent. Product oil is coolingAfter, removing storage tank, solvent desolventizing tank, recycles.

A special purpose device for catalytic extraction coal oil-producing technique, is characterized in that: described catalysisThe special purpose device of extraction coal oil-producing technique, comprises flour mill 1, pulping tank 2, and heater 3,Reactor 4, high-pressure separator 5, low pressure separator 6, vacuum tank 7, solvent recovery tower 8;

Wherein: flour mill 1 is connected with pulping tank 2, pulping tank 2 is connected with heater 3, addsHot device 3 is connected with reactor 4, and reactor 4 is connected with high-pressure separator 5, high-pressure separator5 are connected with low pressure separator 6, and low pressure separator 6 is connected with vacuum tank 7, and vacuum tank 7 connectsConnect with solvent recovery tower 8 and be connected.

Adopt this technology almost can make oily yield reach absolutely, and zero-emission.

Test shows, under absolute pressure 1Kpa condition, temperature of charge is down to 380 DEG C of left and right.Because boiling point significantly reduces, 600～700 DEG C of heavy oil components all gasify.

Advantage of the present invention:

The present invention, in order to solve problems of the prior art, provides a kind of catalytic extraction coal systemOil technology, has simplified production technology, has improved device efficiency, reduced the energy consumption of producing,Material consumption, does not need hydrogen, has reduced pollution, has improved the utilization rate of raw material, has avoided meaninglessConsumption hydrogen, greatly reduce production cost per tone oil. The main difference of the present invention and conventional art is heatingMode difference, conventional tubular heating furnace heats the large temperature difference, little heating surface (area) (HS, and the present invention heats littleThe temperature difference, large heating surface (area) (HS; Reactor types difference, traditional reactor adopts full back-mixing form,Reactor adopts pure axial flow form; Tradition oil product and the flash distillation of coal semicoke secondary are entered under positive pressureOK, oil product and the flash distillation of coal semicoke secondary under vacuum condition, carry out, residual oil product in coal semicokeFew; Tradition coal liquefaction rectifying column adopts liquid phase feeding, rectifying column gas-phase feed of the present invention, rectifyingProcess zero energy consumption.

Technique is simple, device efficiency is high, and reactor volume is little, and the material reaction degree of depth is consistent,Material in full back-mixed reactors, some is because of of short duration basic unreacted of the time of staying, energyConsume lowly, do not need coal generating gas hydrogen making, zero pollution, zero-emission, raw material availability be 100%,The utilization of capacity is high, coal slurry noncoking, adopts heat carrier heating, has reduced material heat intensity, keeps awayExempt from industrial furnace and directly heated the too high critical defect of heat intensity.

Brief description of the drawings

Below in conjunction with drawings and the embodiments, the present invention is further detailed explanation:

Fig. 1 is the special purpose device structural representation of catalytic extraction coal oil-producing technique.

Detailed description of the invention

Embodiment 1

The present embodiment provides a kind of catalytic extraction coal oil-producing technique, it is characterized in that: describedCatalytic extraction coal oil-producing technique, concrete steps are:

First, with flour mill by coal pulverizer to 180 order. Coal fully dissolves in solvent, by solidBody powder type is to coal solution form. Coal dust is delivered to coal dust pot by the mode that adopts gas to carry.Coal dust enters pulping tank from coal dust pot bottom. Pulping tank intermittent stirring formula, makes coal dust and oil abundantBe mixed into coal slurry state. Coal slurry enters tube heater. Heater outlet temperature reaches 450 DEG C,Pressure is 5MPA. Coal dust dissolves completely in solvent, and starts to occur pyrolytic reaction. Coal slurryEnter pure axial flow reactor and become coal solution. It is 5MPA that coal solution remains on 450 DEG C, pressure.The time of staying of coal dust in pure axial flow reactor is 1 hour. Industrial, temperature, be subject toThe heat time is all to control the important means that oil product decomposes the degree of depth. For example ethane cracking furnace is with being heatedTime is controlled the oil product decomposition degree of depth, under the prerequisite of boiler tube noncoking, and high output of ethylene to greatest extent.

Embodiment 2

First, with flour mill by coal pulverizer to 200 order. Coal fully dissolves in solvent, by solidBody powder type is to coal solution form. Coal dust is delivered to coal dust pot by the mode that adopts gas to carry.Coal dust enters pulping tank from coal dust pot bottom. Pulping tank intermittent stirring formula, makes coal dust and oil abundantBe mixed into coal slurry state. Coal slurry enters tube heater. Heater outlet temperature reaches 480 DEG C,Pressure is 8MPA. Coal dust dissolves completely in solvent, and starts to occur pyrolytic reaction. Coal slurryEnter pure axial flow reactor and become coal solution. It is 8MPA that coal solution remains on 480 DEG C, pressure.The time of staying of coal dust in pure axial flow reactor is 1 hour.

Embodiment 3

First, with flour mill by coal pulverizer to 220 order. Coal fully dissolves in solvent, by solidBody powder type is to coal solution form. Coal dust is delivered to coal dust pot by the mode that adopts gas to carry.Coal dust enters pulping tank from coal dust pot bottom. Pulping tank intermittent stirring formula, makes coal dust and oil abundantBe mixed into coal slurry state. Coal slurry enters tube heater. Heater outlet temperature reaches 500 DEG C,Pressure is 10MPA. Coal dust dissolves completely in solvent, and starts to occur pyrolytic reaction. CoalSlurry enters pure axial flow reactor becomes coal solution. Coal solution remains on 500 DEG C, pressure10MPA. The time of staying of coal dust in pure axial flow reactor is 1 hour. 500 DEG C is coalUnder catalyst action, there is the low-temperature space of pyrolytic reaction, only limit to large molecular chain rupture,Tall bond fission; There is not hydrogen migration phenomenon. Coal gas is the product of coal deep decomposition, does not produceCoal gas.

Claims

1. a catalytic extraction coal oil-producing technique, is characterized in that: described catalytic extraction coal systemOil technique, concrete steps are:

First, with flour mill by coal pulverizer to 180～220 order; Coal fully dissolves in solvent,By pressed powder form to coal solution form; Coal dust is delivered to coal dust by the mode that adopts gas to carryTank; Coal dust enters pulping tank from coal dust pot bottom; Pulping tank intermittent stirring formula, makes coal dust and oilFully be mixed into coal slurry state; Coal slurry enters tube heater; Heater outlet temperature reaches450 DEG C～500 DEG C, pressure is 5～10MPA; Coal dust dissolves completely in solvent, and starts to send outRaw pyrolytic reaction; Coal slurry enters pure axial flow reactor becomes coal solution; Coal solution remains on 450DEG C～500 DEG C, pressure are 5～10MPA; The time of staying of coal dust in pure axial flow reactor is 1Individual hour; 450 DEG C～500 DEG C be coal under catalyst action, there is the low-temperature space of pyrolytic reaction,Only limit to large molecular chain rupture, tall bond fission; There is not hydrogen migration phenomenon; Coal gas is coalThe product of deep decomposition, does not produce coal gas;

Enter the flash distillation of high pressure knockout drum from the reaction product decompression out of pure axial flow reactor; HighPress knockout drum top light oil constituents secondary out to reduce pressure, enter rectifier bottoms with gas phase; HighThe reaction product of pressing knockout drum bottom, goes low pressure separation pot;

Reaction product is secondary flash distillation in low pressure separation pot, and the absolute pressure of low pressure separation pot onlyFor 1Kpa; Out heavy oil component of low pressure separation pot top, enters condenser; Condensed changeBecome liquid, flow into vacuum tank; It is coal semicoke that low pressure separation pot bottom does not have the material of gasification, coalSemicoke, after being pumped to cooler, removes coal semicoke storage pool;

The heavy oil component of vacuum tank bottom goes to rectifying column middle part through pump, and vacuum tank top connects vacuumPump; By vavuum pump intrasystem on-condensible gas extract out, emptying; What vavuum pump was extracted out is emptyGas, water vapour;

Enter rectifying column middle part heavy oil component and enter rectifier bottoms light oil constituents and carry out stripping,Rectifying column top out be product oil, rectifier bottoms out be solvent; Product oil is coolingAfter, removing storage tank, solvent desolventizing tank, recycles.

2. a special purpose device for catalytic extraction coal oil-producing technique claimed in claim 1, itsBe characterised in that: the special purpose device of described catalytic extraction coal oil-producing technique, comprise flour mill (1),Pulping tank (2), heater (3), reactor (4), high-pressure separator (5), low pressure separatesDevice (6), vacuum tank (7), solvent recovery tower (8);

Wherein: flour mill (1) is connected with pulping tank (2), pulping tank (2) and heater(3) connect, heater (3) is connected with reactor (4), and reactor (4) and high pressure divideConnect from device (5), high-pressure separator (5) is connected with low pressure separator (6), and low pressure is dividedBe connected with vacuum tank (7) from device (6), vacuum tank (7) connects and solvent recovery tower (8)Connect.