CN104629788A - Complete device for coal liquefaction - Google Patents
Complete device for coal liquefaction Download PDFInfo
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- CN104629788A CN104629788A CN201310567021.7A CN201310567021A CN104629788A CN 104629788 A CN104629788 A CN 104629788A CN 201310567021 A CN201310567021 A CN 201310567021A CN 104629788 A CN104629788 A CN 104629788A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
- C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
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- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a complete device for coal liquefaction. The complete device comprises a slurrying tank, a first reactor, a second reactor serially connected with the first reactor and a fractionating tower; the slurrying tank is connected with the bottom of the first reactor through a high pressure coal slurry pump and a coal slurry preheating furnace; the output end of the first reactor is connected with the input port of the lateral surface of the upper part of the second reactor; and the second reactor is provided with a bottom outlet and a top outlet, the top outlet is connected with a cooling device, the bottom outlet is connected with a decompression device, and the cooling device and the decompression device are connected with the fractionating tower by pipes. The complete device has the characteristics of brief flow, stable operation and high oil yield.
Description
Technical field
The present invention relates to a kind of gelatin liquefaction complexes.
Background technology
At present, DCL/Direct coal liquefaction mainly contains three large techniques in the world: German IGOR technique, U.S. HTI technique and Japanese NEDOL technique.Germany's technique carries out online hydrogenation to the thick oil of liquefaction in high-pressure system, obtains high-quality oil product and hydrogen supply dissolvent, and system device investment is large, and pressure is high, and processing condition are comparatively complicated, and the red mud catalyst activity used is lower; U.S. HTI technique uses outer circulation suspension bed, needs to use recycle pump, and operational condition is quite harsh, even becomes the bottleneck of device steady running; And catalyst costs is high; Japan's process liquefaction reactor adopts bubbling bed, and bottom mineral substance easily deposits, and quality product also will be reprocessed.In addition, Russian technological reaction mild condition, system pressure is low, but the high and catalyst recovery of catalyst costs and early stage coal treatment process numerous and diverse.
CN1438294A proposes the direct coal liquefaction process of a kind of countercurrent ring flow reactor series connection, first in counter-current reactor, carry out mild hydrogenation cracking, first leave system after discharging moisture and aldehydes matter, heavier feeds continues hydrogenation again in loop reactor, obtains higher liquefaction oil yield; CN1587351A is the direct coal liquefaction process that Shenhua Group proposes, and is the modified version of U.S.'s two-stage catalytic liquefaction process, does not also verify through fairly large commerical test.
At present, DCL/Direct coal liquefaction does not also have industrial practice, just at laboratory or Pilot scale runs.Shenhua Group builds first phase of construction Article 1 1,000,000 tons/year of production lines at Inner Mongol E Erduosima family tower, is the first in the world cover industrialization demonstration unit, and what seem especially is meaningful, puts into operation in August, 2009.
DCL/Direct coal liquefaction reactor, as liquefaction process nucleus equipment, directly determines the stability of technical process setting and process operation.Make a general survey of whole coal liquefaction craft, the reactor of use mainly contains bubbling bed, ebullated bed and outer circulation suspension bed three kinds.Comparative maturity or bubbling bed reactor, although there is shortcoming, be applied on full scale plant after all, and in technique of new generation, obtained pilot scale 200t/d verify; On the contrary, improvement done by ebullated bed reactor, i.e. outer circulation suspended-bed reactor, and outer circulation suspended-bed reactor also has to the checking of tens tons of/day scales in pilot scale, and Shanghai 6t/d plant running is also unsatisfactory.The loop reactor that previous patent relates to also does not apply precedent in gelatin liquefaction field.In a word, bubbling bed reactor is the reactor of relative maturity.
From technical process, distillate and solvent hydrofining are connected in high-pressure system by Germany, use fixed bed hydrogenation reactor, and system stability is not enough; The U.S. uses outer circulation floating bed hydrogenation to refine, and does not equally also obtain industry checking, uses the extraction of solvent deliming to improve oily yield; Japan's technique is the independent hydrogenation of circulating solvent.The independent hydrogenation of circulating solvent should be metastable technique.
Summary of the invention
The object of this invention is to provide the gelatin liquefaction complexes that a kind of technical process is simple and clear, running is stable, oily yield is high.
For achieving the above object, the present invention adopts following technical scheme: a kind of gelatin liquefaction complexes, comprise pulping tank, first reactor, with the second reactor and the separation column of the first reactor serial connection, described pulping tank passes through high-pressure coal pulp pump, coal slurry preheating oven connects with the first reactor bottom, the input aperture of the same second reactor upper side of output terminal of the first reactor is connected, described second reactor is provided with outlet at bottom and top exit, described top exit connects with heat sink, described outlet at bottom connects with dropping equipment, described heat sink is connected with separation column by pipeline with dropping equipment.
Described first reactor and the second reactor are bubbling bed reactor.
Described second reactor top is provided with separated space, and its underpart is provided with the gas distributor for deep hydrogenation, and described gas distributor is connected with hydrogen gas compressor by pipeline, and described gas distributor can arrange 1-5.
Described heat sink is two-stage cooling, comprise middle temperature separator, export with middle temperature separator top the low-temperature separator be connected in series, described second reactor head outlet connects with middle temperature separator, described second reactor with between middle temperature separator, middle temperature separator is with being respectively equipped with the first water cooler and the second water cooler between low-temperature separator; Described middle temperature separator bottom outlet is connected with separation column by pipeline, described low-temperature separator top exit divides two-way by pipeline: a road is emptying, another road connects with circulating hydrogen compressor entrance, and described circulating hydrogen compressor outlet is connected with high-pressure coal pulp pump outlet line and hydrogen gas compressor outlet line by pipeline.
Described dropping equipment is two-stage step-down, the vacuum still comprising atmospheric flash tower and be connected in series with it, and described second reactor bottom outlet connects with atmospheric flash tower; Described atmospheric flash tower is connected with separation column by pipeline with vacuum still top output port.
The bottom of described separation column is connected with pulping tank by pipeline, and described pipeline is provided with circulating solvent hydrogenator.
The present invention has following beneficial effect:
The present invention adopts two bubbling bed reactor series connection, and a master once.First reactor is cocurrent flow type, and coal slurry enters from bottom, top discharge directly by the second reactor-side to entering; Second reactor is reverse-flow, and bottom enters hydrogen, and top-down heavier feeds carries out hydrogenation.Second reactor head leaves gas, liquid, Gu separated space, light material leaves system in advance, the reaction mass continuation reaction too much gas of generation or deep reaction is avoided to cause coking, affect oily yield, now light material enters two-stage cooling separation system, namely warm separator and low-temperature separator in, after second reactor bottom material goes out system, through two-stage step-down, i.e. atmospheric flash tower and vacuum still, first material carries out feed separation through reducing pressure into atmospheric flash tower, wherein bottoms material enters vacuum still continuation and reclaims distillate, residue is used for gasification hydrogen-producing, during middle temperature separator bottom cut and the second reactor bottom separation system obtain, heavy ends enters separation column together, distill, obtain light, middle matter cut and bottom heavy ends.In part, matter cut and whole heavy ends enter solvent hydrogenator as circulating solvent and carry out independent hydrogenation, get back to coal slurry preparation system.Distillate enters separation column together with atmospheric flash tower overhead-liquid, reclaims mink cell focus and light middle matter distillate, oily yield is improved as far as possible.
In addition, this low-temperature separator overhead line is used for recover hydrogen, mainly use it for the first reactor and coal slurry mixing carry out mild hydrogenation reaction, remainder can be mixed into the second reactor with fresh hydrogen and react, except as except reaction mass, cooling effect can also be played as cooling material.
Accompanying drawing explanation
Fig. 1 is structural plan of the present invention.
In figure:
1, pulping tank 2, first reactor 3, second reactor 4, middle temperature separator 5, low-temperature separator 6, atmospheric flash tower 7, vacuum still 8, separation column 9, circulating solvent hydrogenator 10, high-pressure coal pulp pump 11, coal slurry preheating oven 12, hydrogen gas compressor 13, circulating hydrogen compressor 14, first water cooler 15, second water cooler 16, gas distributor.
Embodiment
Below in conjunction with accompanying drawing, the invention will be further described.
As seen from Figure 1, the present invention includes pulping tank 1, first reactor 2, be bubbling bed reactor with the second reactor 3 of the first reactor 2 serial connection and the reactor of separation column 8, two serial connection; Second reactor 3 top is provided with separated space, and its underpart is provided with the gas distributor 16 for deep hydrogenation, and gas distributor 16 is connected with hydrogen gas compressor 12 by pipeline, and gas distributor 16 can arrange 1-5 in the second reactor 3 bottom.Pulping tank 1 is connected with bottom the first reactor 2 by high-pressure coal pulp pump 10, coal slurry preheating oven 11, the input aperture of same second reactor 3 upper side of output terminal of the first reactor 2 is connected, second reactor 3 is provided with outlet at bottom and top exit, top exit connects with heat sink, outlet at bottom connects with dropping equipment, and heat sink is connected with separation column 8 by pipeline with dropping equipment.
Heat sink is divided into two-stage to lower the temperature, comprise middle temperature separator 4, export with middle temperature separator 4 top the low-temperature separator 5 be connected in series, second reactor 3 top exit connects with middle temperature separator 4, the second reactor 3 divide with middle temperature answer between device 4, middle temperature separator 4 is with being respectively equipped with the first water cooler 14 and the second water cooler 15 between low-temperature separator 5, middle temperature separator 4 outlet at bottom is connected with separation column 8 by pipeline, low-temperature separator 5 top exit divides two-way by pipeline: a road tail gas is emptying, another road connects with circulating hydrogen compressor 13 entrance, circulating hydrogen compressor 13 is exported and is connected with high-pressure coal pulp pump 10 outlet line and hydrogen gas compressor 12 outlet line by pipeline, such layout pipeline be in order to recover hydrogen is used for the first reactor 2 and coal slurry mixing carry out mild hydrogenation reaction, the gas distributor 16 that the recover hydrogen of remainder can be mixed into the second reactor 3 bottom with fresh hydrogen carries out deep hydrogenation reaction, in addition, cooling effect can also be played as cooling material.
Dropping equipment is divided into two-stage step-down, comprises atmospheric flash tower 6 and vacuum still 7, second reactor 3 outlet at bottom that is connected in series with it connects with atmospheric flash tower 6; Atmospheric flash tower 6 is connected with separation column 8 by pipeline with vacuum still 7 top output port.In addition, the bottom of separation column 8 is connected with pulping tank 1 by pipeline, and pipeline is provided with circulating solvent hydrogenator 9.
Concrete technology flow process is as follows:
The coal slurry prepared is mixed into the first reactor 2 through the hydrogen of high-pressure coal pulp pump 10 and recovery, the second reactor 3 top is entered from side direction after preliminary hydrogenation reaction, material first carries out gas at the separated space on the second reactor 3 top, liquid, Gu three phase separation, gas phase portion is flowed out by the second reactor 3 top exit, middle temperature separator 4 is entered after one-level cooling, temperature controls at 200-250 DEG C, matter distillate in recovery part, residual gas continues to enter low-temperature separator 5 mutually after secondary cooling, reclaim unreacting gas, light ends enters the refining processing of subsequent processing after the outlet at bottom of low-temperature separator 5 directly reclaims, through circulating hydrogen compressor 13 times the first reactors 2 after gas fraction emptying, the separated space of the second reactor 3 through its top remains liquid-solid material slowly descending after being separated, and fully contacts and carries out deep hydrogenation reaction, improve oily yield with the fresh hydrogen entered from bottom and the miscellany that remains recover hydrogen.After deep hydrogenation, reacting rear material flows out from the second reactor 3 outlet at bottom, enters atmospheric flash tower 6 be separated through decompression, and after cutting out partial liquid, residue is difficult to separation of material, and continuation decompression enters vacuum still 7 and reclaims distillate further; Enter separation column 8 from the distillate of vacuum still 7 recovery together with the distillate reclaimed by atmospheric flash tower 6 and middle temperature separator 4 and carry out fractionation, and remaining be difficult to react residue and catalyzer and reaction after together with mineral substance as residue, wait until hydrogen manufacturing.Separation column 8 fractionate out light ends and in, heavy ends three kinds, in light ends and major part, matter cut is as the refining processing of thick product introduction subsequent processing, and matter cut and whole heavy endss are transported to circulating solvent hydrogenator 9 as circulating solvent and carry out solvent hydrogenation in part, circulating solvent returns in pulping tank 1.
The foregoing is only preferred embodiment of the present invention, not in order to limit the present invention, within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (6)
1. gelatin liquefaction complexes, comprise pulping tank, the first reactor, with first reactor serial connection the second reactor and separation column, described pulping tank is connected with the first reactor bottom by high-pressure coal pulp pump, coal slurry preheating oven, it is characterized in that: the input aperture of the same second reactor upper side of output terminal of the first reactor is connected, described second reactor is provided with outlet at bottom and top exit, described top exit connects with heat sink, described outlet at bottom connects with dropping equipment, and described heat sink is connected with separation column by pipeline with dropping equipment.
2. gelatin liquefaction complexes according to claim 1, is characterized in that: described first reactor and the second reactor are bubbling bed reactor.
3. gelatin liquefaction complexes according to claim 1, it is characterized in that: described second reactor top is provided with separated space, its underpart is provided with the gas distributor for deep hydrogenation, described gas distributor is connected with hydrogen gas compressor by pipeline, and described gas distributor can arrange 1-5.
4. gelatin liquefaction complexes according to claim 3, it is characterized in that: described heat sink is two-stage cooling, comprise middle temperature separator, export with middle temperature separator top the low-temperature separator be connected in series, described second reactor head outlet connects with middle temperature separator, described second reactor with between middle temperature separator, middle temperature separator is with being respectively equipped with the first water cooler and the second water cooler between low-temperature separator; Described middle temperature separator bottom outlet is connected with separation column by pipeline, described low-temperature separator top exit divides two-way by pipeline: a road is emptying, another road connects with circulating hydrogen compressor entrance, and described circulating hydrogen compressor outlet is connected with high-pressure coal pulp pump outlet line and hydrogen gas compressor outlet line by pipeline.
5. according to the arbitrary described gelatin liquefaction complexes of claim 1-4, it is characterized in that: described dropping equipment is two-stage step-down, the vacuum still comprising atmospheric flash tower and be connected in series with it, described second reactor bottom outlet connects with atmospheric flash tower; Described atmospheric flash tower is connected with separation column by pipeline with vacuum still top output port.
6. gelatin liquefaction complexes according to claim 5, it is characterized in that: the bottom of described separation column is connected with pulping tank by pipeline, described pipeline is provided with circulating solvent hydrogenator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310567021.7A CN104629788A (en) | 2013-11-15 | 2013-11-15 | Complete device for coal liquefaction |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310567021.7A CN104629788A (en) | 2013-11-15 | 2013-11-15 | Complete device for coal liquefaction |
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| CN104629788A true CN104629788A (en) | 2015-05-20 |
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| CN201310567021.7A Pending CN104629788A (en) | 2013-11-15 | 2013-11-15 | Complete device for coal liquefaction |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105181732A (en) * | 2015-10-15 | 2015-12-23 | 神华集团有限责任公司 | Evaluation device and evaluation method for coal direct liquification performance |
| CN108106460A (en) * | 2016-11-24 | 2018-06-01 | 神华集团有限责任公司 | The cooling system and method for a kind of coal directly-liquefied residue |
| CN109054903A (en) * | 2018-08-24 | 2018-12-21 | 新奥科技发展有限公司 | A kind of coal hydrogenation gasification method and device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1438294A (en) * | 2003-02-14 | 2003-08-27 | 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 |
| CN1869159A (en) * | 2006-06-27 | 2006-11-29 | 神华集团有限责任公司 | Method of directly liquifying coal |
-
2013
- 2013-11-15 CN CN201310567021.7A patent/CN104629788A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1438294A (en) * | 2003-02-14 | 2003-08-27 | 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 |
| CN1869159A (en) * | 2006-06-27 | 2006-11-29 | 神华集团有限责任公司 | Method of directly liquifying coal |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105181732A (en) * | 2015-10-15 | 2015-12-23 | 神华集团有限责任公司 | Evaluation device and evaluation method for coal direct liquification performance |
| CN105181732B (en) * | 2015-10-15 | 2018-08-07 | 神华集团有限责任公司 | The evaluating apparatus and evaluation method of DCL/Direct coal liquefaction performance |
| CN108106460A (en) * | 2016-11-24 | 2018-06-01 | 神华集团有限责任公司 | The cooling system and method for a kind of coal directly-liquefied residue |
| CN109054903A (en) * | 2018-08-24 | 2018-12-21 | 新奥科技发展有限公司 | A kind of coal hydrogenation gasification method and device |
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