CN1803985A - Magnetic scraper loop reactor for coal direct liquefaction and coal direct liquefaction method thereof - Google Patents
Magnetic scraper loop reactor for coal direct liquefaction and coal direct liquefaction method thereof Download PDFInfo
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- CN1803985A CN1803985A CN 200510097409 CN200510097409A CN1803985A CN 1803985 A CN1803985 A CN 1803985A CN 200510097409 CN200510097409 CN 200510097409 CN 200510097409 A CN200510097409 A CN 200510097409A CN 1803985 A CN1803985 A CN 1803985A
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Abstract
The related loop reactor for coal direct liquefaction comprises: an outside cylinder, a central tube, a gas distributor, a plurality of magnetic scrapers arranged equally between the cylinder and tube, a magnetic draw device, and a device frame. This invention improves material loop speed and turbulence strength to avoid coking and raise heat/mass transfer efficiency for wide application.
Description
Technical field
The present invention relates to the DCL/Direct coal liquefaction field, particularly relate to a kind of magnetic scraper loop reactor for coal direct liquefaction and coal direct liquefaction method thereof.
Background technology
The world's three big basic power sources are from solid mineral fuel coal, petroleum and natural gas.Coal is the abundantest in the world solid mineral fuel, be distributed in countries in the world, for example there are storage in bulk and exploitation in China, North America, Australia, South Africa, Russia, Europe etc., yet people are used as fuel with solid raw coal form always, seldom process refining, its major cause coal is a solid, and the image-stone oil and gas is not easily processed refining and transportation; Contain a large amount of sulphur and nitrogen and so on impurity in the raw coal, when being used as fuel with the raw coal form, produce a large amount of obnoxious flavoures and impurity, contaminate environment causes big area acid rain, the harm humans living environment.Foreign matter content in the solid raw coal, moisture content, physical property, calorific value and combustioncharacteristics etc. are along with different coal breed differences are very big, the chemical structure of coal own is extremely complicated, molecule is with monocycle in the coal, dicyclo, cyclic aromatic compounds such as three rings, particularly the macromole of condensed-nuclei aromatics or heterocyclic arene is formed, this ring texture macromolecular structure is stable, be difficult to pyrolysis liquefying, and carbon content in coal is than little, for example Sweet natural gas (methane) ratio of carbon-hydrogen 4, oil is about 2: 1, and coal is generally less than 1: 1, so will make gelatin liquefaction must rely on the outside that hydrogen or hydrogen donor are provided, otherwise can only obtain coke, a small amount of tar and coke(oven)gas.
Along with but the recover petroleum resource reduces day by day, oil price rises steadily, and people attempt the coal that storage is abundant and are transformed into and are convenient to transport the synthetic liquid fuel that can match in excellence or beauty with oil with the calorific value height, and countries in the world are developed the gelatin liquefaction technology one after another.Exploitation gelatin liquefaction Technology Need drops into many, the complex structure of the device category in the coal liquification device, technical requirements height in a large number.In DCL/Direct coal liquefaction technology, liquefying reactor is one of nucleus equipment of whole liquefaction process, and in the DCL/Direct coal liquefaction technology of developed country's exploitation at present, liquefying reactor adopts bubbling bed reactor or pump circulation suspended-bed reactor.Wherein there is the bubble skewness in bubbling bed reactor, and the bubble short circuit phenomenon is arranged, and gas holdup is higher, and the reactor useful volume is less than normal, the fluid flow disorder, and superficial liquid velocity is less vertically.Coal might be located to take place to assemble or coking phenomenon in hydrogenation process at reactor bottom and wall etc.The pump circulation suspended-bed reactor mainly depends on external recycle pump, reach reaction mass circulation and well-mixed purpose, because recycle pump is operated under High Temperature High Pressure, the operational conditions harshness, the cost of keeping steady running is higher, risk is bigger, since the system solid content height of handling, the recycle pump serious wear, and operation difficulty steady in a long-term is bigger.
Summary of the invention
The objective of the invention is to overcome above-mentioned prior art gelatin liquefaction reactor exists not enough, be engaged in the development research and the practice of gelatin liquefaction technology for a long time through the contriver, develop a kind of speed of circulation and turbulence intensity that improves material, can avoid coking phenomenon that the magnetic scraper loop reactor for coal direct liquefaction that heat and mass transfer efficient is higher takes place.
Another object of the present invention is to provide a kind of method of new DCL/Direct coal liquefaction.
Magnetic scraper loop reactor for coal direct liquefaction provided by the invention is characterized in that comprising urceolus 1, and urceolus is pipe or cylinder, and two ends are hemispherical head, is respectively equipped with discharge port 7 and opening for feed 3; Pipe core 4 is a pipe, there is certain distance its upper end and bottom with hemispherical head respectively, external diameter is less than the internal diameter of urceolus, pipe core makes reaction mass along rising in the pipe core, make full use of the buoyancy of raw hydrogen and the kinetic energy of import coal oil mixture, make reaction mass in pipe core on flow, and flow downward in the interannular formation of pipe core and urceolus; Because the interannular bubble is less, cause the interannular material density greater than the material density in the pipe core, density difference further promotes the circulation movement of material, make interannular fluidic circulation velocity increase, prevent coal dust coking in hydrogenation process, obtain higher speed of circulation and turbulence intensity simultaneously, improved heat transfer, mass-transfer efficiency.
Gas distributor 2 is arranged on pipe core bottom central authorities, is the orifice-plate type gas distributor, and the hydrogen of charging and coal oil mixture uniform distribution are entered in the reactor.
Magnetic scraper is a plurality of, is preferably 2-3, is annular, and its section is triangular in shape, and its external diameter is slightly less than the urceolus internal diameter, and impartial up and down freely being arranged between urceolus and pipe core located it by magnetic force, moves up and down under Magnetic force tracting; Magnetic force tracting device 6 is a permanent magnet, is located on the outside wall surface of urceolus, joins by Magnetic force tracting appliance stand 8 and track, can move up and down along track, Magnetic force tracting appliance stand 8 is that (mini-reactor is two, presses circumference 180 degree and gets final product at interval for two or three screw rod tracks; Large-scale reactor can have three, and at interval 120 degree are placed), be listed in respectively reactor around.Electric device and built-in rotation screw are arranged on the Magnetic force tracting device, thereby the short transverse of traction permanent magnetic body in the reactor outside moves.Magnetic scraper can be scraped up and down and get outer tube inner wall under the traction of Magnetic force tracting device back and forth, effectively prevents the coking of wall, guarantees the long-term stability operation of magnetic knife loop reactor.
The invention provides a kind of coal direct liquefaction method, comprising:
(1) coal dust is made pumpable coal slurry with the ferrum-based catalyst (seeing CNl579623A) of hydrogenation circulating solvent and high dispersive, through the high-pressure coal pulp pump and the H that partly circulates
2Mix post-heating to 350-450 ℃;
(2) coal slurry after the preheating enters from first section counter-current reactor top, the recycle gas after the compressed preheating, wherein H
2Concentration is 60-80%, enter from the bottom and to form adverse current with coal slurry and carry out hydrogenation liquefaction, temperature of reaction is 400-450 ℃, the partial liquefaction product carries out gas-liquid separation by entering first high-temperature separator after the water cooler cooling together with recycle gas, divided gas flow recycles as recycle gas, You Heshui in the liquid sends to further separation, and water is sent to treatment unit for waste water and handles, and oil enters online hydrogenator after dephenolize;
(3) discharge material by first section counter-current reactor bottom, with fresh H
2After compression with circulation H
2Enter second section magnetic scraper loop reactor by the bottom together after the mixing preheating and carry out coal hydrogenation liquefaction, temperature of reaction is 400-470 ℃, H
2Concentration is 75-95%, and preferred 85-90% liquefied product is isolated top stream material through second high-temperature separator again after cooling, and underflow materials is removed residue through underpressure distillation and entered online hydrogenator together;
(4) enter online hydrogenator with unitary overhead oil of underpressure distillation and second high-temperature separator top stream material and carry out shortening from taking off oil behind the phenol, the liquid that warm separator is separated in the hydrogenation reaction product warp removes to prepare coal slurry as circulating solvent, gas phase enters low-temperature separator through water cooler and separates, the gas that leaves low-temperature separator removes first section counter-current reactor through purifying the rear section, major part is removed second section magnetic scraper ring loop reactor, liquefaction oil goes to the air distillation unit to obtain gasoline fraction, fraction of diesel oil respectively.
Coal direct liquefaction method provided by the invention has two recycle hydrogen loops, and first circulation loop is the center with first section counter-current reactor, and hydrogen concentration is low to be 60-80%; Second circulation loop is the center with second section magnetic scraper ring loop reactor and online hydrogenator, and hydrogen concentration is higher to be 75-95%, makes the hydrogen concentration of second section magnetic scraper ring loop reactor bring up to 85-90%.
Oxygen hydrogenation in the gelatin liquefaction process in the coal generates the reaction of water mainly to carry out in first section counter-current reactor, the water that generates through first high-temperature separator after, leave the gelatin liquefaction reactive system very soon, the content that enters water in the material of online hydrogenator like this significantly reduces, the work atmosphere of the online hydrogenation catalyst in the online hydrogenator of gelatin liquefaction obtains essence ground to be improved, thereby make the steady running for a long time of online hydrogenator, the solvent that obtains has good hydrogen supply performance, and liquefaction oil is by more stable forming.It is shorter at reactor residence time that adverse current provided by the invention, circulation, the placed in-line coal direct liquefaction method of online hydrogenator can better satisfy the lightweight liquiefied product of gelatin liquefaction reaction simultaneously, difficult liquefaction coal and heavy Coal Liquefaction Products have higher rate of mass transfer and the requirement in long reaction times at reactor residence time than length and with gas phase hydrogen, improve the gelatin liquefaction reaction efficiency, increase gelatin liquefaction liquid yield (referring to CNl438294A).
Magnetic scraper loop reactor for coal direct liquefaction provided by the invention and liquifying method characteristics thereof are carried out second-stage reaction in magnetic scraper loop reactor, magnetic scraper loop reactor novel structure uniqueness, circulate effective up and down, speed of circulation and turbulence intensity had both been improved, can effectively eliminate coking phenomenon again, have heat transfer, characteristics that mass-transfer efficiency is high, thereby realized changing the long-period stable operation of reactor.This reactor and liquifying method are simple to operate, Coal Liquefaction Products yield height, special light-end products yield height.
Description of drawings
Fig. 1 is the magnetic scraper loop reactor structural representation
Fig. 2 magnetic scraper structure sectional view
Embodiment
The present invention further specifies the present invention with the following example, but protection scope of the present invention is not limited to the following example.
Embodiment 1:
At the gas-liquid system, with the atmospheric air is gaseous media, liquid phase medium is distilled water-Span system, the coal oil mixture character basically identical under its density and viscosity and the real reaction condition, and experiment is respectively bubbling bed liquefying reactor and magnetic scraper loop reactor with reactor.Wherein, the urceolus internal diameter of bubbling bed liquefying reactor is 0.07m, and total reactor height 2.0m, reactor are flat, and no pipe core, sparger are the blank pipe of internal diameter 6mm, and the sparger pelvic outlet plane flushes with the bottom surface.The urceolus diameter of magnetic scraper loop reactor is 0.07m, inner diameter of centerpipe is 0.045m, wall thickness 5mm, total reactor height 2.0m, reactor are flat, and the pipe core height is 1.8m, apart from end height is 5mm, the interannular width is 7.5mm, and sparger is the blank pipe of internal diameter 6mm, and the sparger pelvic outlet plane flushes with the bottom surface.
Be respectively 2,3,4,5,6 at operating gas velocity, under the condition of 7L/min, the top number of bubbles of bubbling bed liquefying reactor is more, the bottom number of bubbles is less, bubble distributes very inhomogeneous, bubble in tower by the time have from the phenomenon of tower medullary ray short circuit and take place; And can form the intensive circulation movement in the magnetic scraper loop reactor, and bubble is evenly distributed, and bubble has long movement path in reactor, and the residence time is long, and circulation liquid speed is big.Judge that from flow-pattern magnetic scraper loop reactor obviously is better than bubbling bed liquefying reactor.
The Klorvess Liquid that with concentration is 0.4mol/L is made tracer agent, adopts conductometric titration, and computer sampling is measured the liquid circulation flow velocity.Be respectively 2,3,4,5,6 at operating gas velocity, under the condition of 7L/min, the circulation velocity of bubbling bed liquefying reactor is respectively 0.0081,0.0095,0.010,0.011,0.012,0.012m/s; The circulation velocity of magnetic scraper loop reactor is respectively 0.15,0.19,0.28,0.39,0.45,0.49m/s, increases 75.5%-94.6% than bubbling bed liquefying reactor.
Embodiment 2:
At the gas-liquid system, with the atmospheric air is gaseous media, liquid phase medium is distilled water-Span system, the coal oil mixture character basically identical under its density and viscosity and the real reaction condition, and experiment is respectively bubbling bed liquefying reactor and magnetic scraper loop reactor with reactor.Wherein, the urceolus internal diameter of bubbling bed liquefying reactor is 0.07m, and total reactor height 2.0m, reactor are flat, and no pipe core, sparger are that the aperture is the orifice plate sparger of 1mm, and the sparger pelvic outlet plane flushes with the bottom surface.Add a small amount of thickness in the liquid-phase system, be easy to be attached on the greasy dirt of outer tube inner wall face.
Urceolus 1 diameter of band magnetic scraper loop reactor (as Fig. 1) is 0.07m, pipe core 3 internal diameters are 0.045m, wall thickness 5mm, total reactor height 2.0m, reactor are flat, and the pipe core height is 1.8m, apart from end height is 5mm, the interannular width is 7.5mm, and gas distributor 2 is the orifice plate sparger of 1mm for the aperture, and the sparger pelvic outlet plane flushes with the bottom surface; The outer tube inner wall design has magnetic scraper 5, and Magnetic force tracting device 5 is installed on the outer drum outer wall.
Under normal running gas speed, open the magnetic force wall scraper, magnetic scraper moves up and down with the Magnetic force tracting device on the outer wall, will wipe off attached to the heavy-gravity greasy dirt on the outer tube inner wall face, the cleaning that has kept inwall has effectively prevented the coking phenomenon that will take place under the actual response condition; The operation of magnetic force wall scraper is normal, is easy to safeguard.
Embodiment 3:
Experiment adopts a kind of young bituminous coal the results are shown in table 1 with the identical first section counter-current reactor of embodiment 1 and liquefaction result and a kind of young bituminous coal of second section magnetic scraper loop reactor and the placed in-line coal direct liquefaction method of online hydrogenator in the liquefaction of traditional coal liquefaction craft of two placed in-line reactors of bubbling bed.
Table 1
| The counter-current reactor temperature of reaction | The loop reactor temperature of reaction | Hydrogen consumption % | Oil yield % | Gas yield % | Aquatic products rate % | |
| Liquifying method of the present invention | 440℃ | 460℃ | 7.0 | 58.5 | 14.5 | 8.6 |
| The tradition liquefaction process | 450℃ | 450℃ | 8.7 | 54.3 | 22.0 | 8.9 |
Embodiment 4:
A kind of Chinese brown coal the results are shown in table 2 with the liquefaction result of embodiment 1 identical first section counter-current reactor, second section magnetic scraper loop reactor and the placed in-line coal direct liquefaction method of online hydrogenator and a kind of liquefaction of Chinese brown coal tradition liquefaction process.
Table 2
| The counter-current reactor temperature of reaction | The loop reactor temperature of reaction | Hydrogen consumption % | Oil yield % | Gas yield % | Aquatic products rate % | |
| Liquifying method of the present invention | 430℃ | 455℃ | 8.1 | 58.5 | 15.5 | 20.1 |
| The tradition liquefaction process | 450℃ | 450℃ | 9.5 | 50.6 | 22.4 | 22.7 |
Claims (5)
1, a kind of magnetic scraper loop reactor for coal direct liquefaction is characterized in that comprising urceolus (1), and urceolus is cylinder or pipe, and two ends are hemispherical head, is respectively equipped with discharge port (7) and opening for feed (3); Pipe core (4) is a pipe, and there is certain distance its upper end and bottom with hemispherical head respectively, and external diameter is less than the internal diameter of urceolus; Gas distributor (2) is arranged on pipe core bottom central authorities, is the orifice plate sparger; Magnetic scraper (5) is a plurality of, is annular, and its section is triangular in shape, and its external diameter is slightly less than the urceolus internal diameter, and impartial up and down freely being arranged between urceolus and pipe core located it by magnetic force; Magnetic force tracting device (6) is a permanent magnet, is located on the outside wall surface of urceolus to join with Magnetic force tracting appliance stand (8) track.
2,, it is characterized in that described magnetic scraper is 2-3 according to the magnetic scraper loop reactor for coal direct liquefaction of claim 1.
3, a kind of coal direct liquefaction method comprises
(1) coal dust is made pumpable coal slurry with the ferrum-based catalyst of hydrogenation circulating solvent and high dispersive, through the high-pressure coal pulp pump and the H that partly circulates
2Mix post-heating to 350-450 ℃;
(2) coal slurry after the preheating enters from first section counter-current reactor top, the recycle gas after the compressed preheating, wherein H
2Concentration is 60-80%, enter from the bottom and to form adverse current with coal slurry and carry out hydrogenation liquefaction, temperature of reaction is 400-450 ℃, the partial liquefaction product carries out gas-liquid separation by entering first high-temperature separator after the water cooler cooling together with recycle gas, divided gas flow recycles as recycle gas, You Heshui in the liquid sends to further separation, and water is sent to treatment unit for waste water and handles, and oil enters online hydrogenator after dephenolize;
(3) discharge material by first section counter-current reactor bottom, with fresh H
2After compression with circulation H
2Enter second section magnetic scraper loop reactor by the bottom together after the mixing preheating and carry out coal hydrogenation liquefaction, temperature of reaction is 400-470 ℃, H
2Concentration is 75-95%, and liquefied product is isolated top stream material through second high-temperature separator again after cooling, and underflow materials is removed residue through underpressure distillation and entered online hydrogenator together;
(4) enter online hydrogenator with unitary overhead oil of underpressure distillation and second high-temperature separator top stream material and carry out shortening from taking off oil behind the phenol, the liquid that warm separator is separated in the hydrogenation reaction product warp removes to prepare coal slurry as circulating solvent, gas phase enters low-temperature separator through water cooler and separates, the gas that leaves low-temperature separator removes first section counter-current reactor through purifying the rear section, major part is removed second section magnetic scraper loop reactor, liquefaction oil goes to the air distillation unit to obtain gasoline fraction, fraction of diesel oil respectively.
4, according to the coal direct liquefaction method of claim 3, it is characterized in that first section counter-current reactor is bubbling bed reactor, online hydrogenator is a fixed bed hydrogenation reactor.
5,, it is characterized in that H in second section magnetic scraper loop reactor according to the method for the DCL/Direct coal liquefaction of claim 3
2Concentration be 85-90%.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2005100974090A CN100338179C (en) | 2005-12-28 | 2005-12-28 | Magnetic scraper loop reactor for coal direct liquefaction and coal direct liquefaction method thereof |
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| CNB2005100974090A CN100338179C (en) | 2005-12-28 | 2005-12-28 | Magnetic scraper loop reactor for coal direct liquefaction and coal direct liquefaction method thereof |
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| CN100338179C CN100338179C (en) | 2007-09-19 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102010741A (en) * | 2010-11-26 | 2011-04-13 | 煤炭科学研究总院 | Method for directly liquefying coals with function of maximizing utilization of liquefied residues |
| RU2448149C1 (en) * | 2010-12-20 | 2012-04-20 | Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") | Plant for combined cleaning of furnace coil and transfer pipeline from coke deposits |
| CN108531217A (en) * | 2017-03-01 | 2018-09-14 | 何巨堂 | The separation method of the hydrocarbon material hydrogenation reactor three-phase product of drain cooling-down type |
| CN109554185A (en) * | 2017-09-25 | 2019-04-02 | 神华集团有限责任公司 | Coal carries out the method and apparatus of liquefaction reaction and the method and system of DCL/Direct coal liquefaction production oil product |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3943036C2 (en) * | 1989-12-27 | 1994-03-10 | Gfk Kohleverfluessigung Gmbh | Process for the hydrogenation of a carbon-containing feed, in particular coal and / or heavy oil |
| US5045180A (en) * | 1990-04-16 | 1991-09-03 | Hri, Inc. | Catalytic two-stage coal liquefaction process having improved nitrogen removal |
| CN1171667C (en) * | 2002-02-01 | 2004-10-20 | 中国石油天然气股份有限公司 | Multi-stage circular flow reactor |
| CN1506152A (en) * | 2002-12-06 | 2004-06-23 | 中国石油天然气股份有限公司 | Circulating reactor with new-type internal member |
| CN1243813C (en) * | 2003-02-14 | 2006-03-01 | 煤炭科学研究总院北京煤化学研究所 | Coal directly-liquifying process with series counter-current and circulating coal-liquifying reactor |
-
2005
- 2005-12-28 CN CNB2005100974090A patent/CN100338179C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102010741A (en) * | 2010-11-26 | 2011-04-13 | 煤炭科学研究总院 | Method for directly liquefying coals with function of maximizing utilization of liquefied residues |
| CN102010741B (en) * | 2010-11-26 | 2013-04-10 | 煤炭科学研究总院 | Method for directly liquefying coals with function of maximizing utilization of liquefied residues |
| RU2448149C1 (en) * | 2010-12-20 | 2012-04-20 | Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") | Plant for combined cleaning of furnace coil and transfer pipeline from coke deposits |
| CN108531217A (en) * | 2017-03-01 | 2018-09-14 | 何巨堂 | The separation method of the hydrocarbon material hydrogenation reactor three-phase product of drain cooling-down type |
| CN109554185A (en) * | 2017-09-25 | 2019-04-02 | 神华集团有限责任公司 | Coal carries out the method and apparatus of liquefaction reaction and the method and system of DCL/Direct coal liquefaction production oil product |
| CN109554185B (en) * | 2017-09-25 | 2023-10-03 | 国家能源投资集团有限责任公司 | Method and device for performing liquefaction reaction on coal and method and system for directly liquefying coal to produce oil |
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