CN107849460A - Direct coal liquefaction technique and system - Google Patents
Direct coal liquefaction technique and system Download PDFInfo
- Publication number
- CN107849460A CN107849460A CN201680040816.4A CN201680040816A CN107849460A CN 107849460 A CN107849460 A CN 107849460A CN 201680040816 A CN201680040816 A CN 201680040816A CN 107849460 A CN107849460 A CN 107849460A
- Authority
- CN
- China
- Prior art keywords
- reactor
- slurry
- hydrogen
- cut
- fed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
-
- 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
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
- C10G1/086—Characterised by the catalyst used
-
- 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
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/06—Vacuum distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of direct coal liquefaction technique and system, it produces the jet fuel/diesel oil or laboratory raw material of maximum output using the recycling of dispersed catalyst and normal pressure and vacuum fractionater bottoms, while eliminates all slurry heat exchangers and slurry preheating furnace.In a heat exchanger and the pre-heating process hydrogen in hydrogen furnace, the normal pressure and vacuum fractionater bottoms for making the recycling of input of the technique hydrogen with being just fed to direct liquefaction reactor mix if necessary.The heat for hydrogen heat exchanger is provided by the extra duty from heat separator, the heat separator receives effluent from the direct liquefaction reactor.Product selectivity is controlled by operating condition.
Description
Technical field
The present invention relates to direct coal liquefaction (direct coal liquefaction, DCL) technique and system, pass through hydrogenation
Coal is converted into fuel and chemical products.Coal liquefaction occurs at 100 to 1000 bars and 400 to 520 DEG C.
Background technology
In DCL methods, coal is made logical conventional process derivative solvent into slurry and pump is pressurized to operating pressure.Generally,
Slurry is heated to by operating condition by heat exchanger or baking furnace.Heat for heat exchange is generally by during coal liquefaction
Heat of reaction provides.In some techniques, in the technique by prepare part hydrogenation solvent (donor solvent) and/or
Release additional heat during liquiefied product is promoted to a higher rank, to remove sulphur, nitrogen and oxygen.
In history, in known DCL techniques, the ratio between coal and slurry is maximized.For example, U.S.4,944,866 is old
State " using only technique derived product, as in the technique of slurry, a target is to increase as much as possible between coal and slurry
Ratio, so as to make the expensive reaction compartment of liquid-phase hydrogenation keep it is smaller ".
Slurry preheating furnace is used in most patent techniques.Because the temperature of mixed slurry derives solvent phase due to thermal process
It is restricted for the low ratio of the quantity of environment temperature coal, so needing slurry preheating furnace.In addition, use donor solvent
And/or the technique of low activity catalyst needs to be preheating to the temperature close to liquefaction condition, to start liquefaction reaction.These factors
Combination cause to need expensive big preheating furnace.
" main liquefaction step is integrated into by hydrotreating in Graeser et al. using another problem of slurry preheating furnace
Promote to a higher rank coal derived oils (Upgrading of Coal Derived Oil by Integrating Hydrotreatment to
The Primary Liquefaction Step) " in discuss, wherein statement is to firing slurry preprocessor system " for deposition
It is very sensitive with coke formation, especially present in preheater tube under high temperature ".
Similarly, in U.S.4,666,589, author's statement is to " it is known that the oily coal-slurry oil material of fine-powdered coal and slurry
It is the recycling distillate flow of the operation from coal liquefaction craft, it undergoes swelling level during heating ".
And in addition, " the section due to the initial heat exchange device and preheater for slurry and hydrogen mixture it
Between swell process cause viscosity to dramatically increase.Viscosity increase can cause significantly to press in the case of in the absence of special safeguard procedures
Drop ".In addition, author's statement to " when in the three-phase mixture of heating coal/slurry oil material in the case of hydrogen-containing gas being present, can be
The precipitation of solid constituent occurs in the heat-exchanger pipeline of preheater ".In this patent, inventor propose using heat exchanger and
The combination of stove preheats hydrogenated gas and slurry simultaneously.
In U.S.4,473,460, description preheats slurry and hydrogen using multiple heat exchangers in the normal operation period,
Reactant is pre-heated to reactor temperature without slurry preheating furnace.In this specified scheme, from liquefying and promote to a higher rank two
Person produces heat.
The content of the invention
The present invention is the improvement of the technique described in US application case 14/147,542 (WO 2014/110085Al), in it
Appearance is incorporated herein in entirety by reference.
According to the present invention, 600 of the sufficient amount from normal pressure fractioning pipestill (Atmospheric Pipestill, APS)
To 700 ℉+(316 to 371 DEG C+) (nominally 650 ℉+) cut and from electron tubes type distillation still (Vacuum
Pipestill, VPS) 650 to 950/1100 ℉ (343 to 510/593 DEG C -) (nominally 650 to 1000 ℉) cut in slurry
Mixed in mixing channel with feed coal so that the temperature of slurry is at least 600 ℉ (316 DEG C).Nominal 650 to 1000 from VPS
It is oily (vacuum gas oil, VGO) that ℉ cuts are frequently referred to vacuum gas.
Slurry from slurry mixing tanks mixes with being pre-heated to the hydrogen of a temperature, and the temperature to be fed to
Combined slurry/hydrogen of liquefying reactor is at least about 660 ℉ (349 DEG C) and is preferably ranges between 660 and 700 ℉ (349-
371 DEG C) at a temperature of between.This technique flow arrangement has the advantages of following extremely important：Eliminate to slurry heat exchanger or slurry
Expect the demand of preheater, and then eliminate high surface area slurry heat exchanger, high surface area preheating furnace, coking and solid deposition and ask
Topic, and the increase of cost.
Or VGO can also replace the quenching that normal hydrogenated gas is used in liquefying reactor.This is eliminated to liquefying reactor
Between extra process gas compression requirements and also reduce reactor in superficial gas velocity, therefore reduce reactor in gas
It is detained.In alternative configuration, can be removed VGO part as product.Another alternative solution is using enrichment VGO and H2Place
Process gases is quenched.Under all case above, VPS size should be set to that producing bottoms removes stream with from system
Remove ash content.
According to another aspect of the present invention, VPS bottoms (1000 to 1100 ℉+) are also recyclable mixes to slurry
Groove, with provide promote slurry mixing tanks temperature be increased at least 600 ℉+enough heats, so as to increase liquefying reactor entrance
The catalyst concn at place.
Brief description of the drawings
The schematic diagram for the direct coal liquefaction system that Fig. 1 is applied in the embodiment described of the present invention.
Embodiment
The present invention DCL techniques reach in the case of without slurry heat exchanger or slurry preheating furnace high coal conversion ratio and
Liquid yield.As illustrated in Figure 1, by APS bottoms and VGO recycling and hydrogen processing gas heat exchanger and
Preheating furnace, which is reached, is input to liquefied all heats.
The embodiment for being used to perform the reactor assembly of direct coal liquefaction according to the present invention is shown in Fig. 1.In conventional gas
Blow the moisture that coal is fed in formula tumbling mill (not shown) and dries and pulverizes to 1% to 4%.By through pulverizing and drying
Coal 25 is fed in slurry mixing tanks 26 with scattered catalyst 30, in the mixing channel 26, itself and 600 from APS 16
To one of 700 ℉+(316 to 371 DEG C+) (nominally 650 ℉+) cut 2 and the bottoms 1 optionally from VPS 28
Point (APS and VPS are even more typically referred to as atmospheric fractionator and vacuum fractionater respectively) mixing, and with from pipeline 17
VGO mixing, so as to form stream of slurry.
Catalyst in the illustrated embodiment preferably in 2-10% phosphomolybdic acids (phosphomolybdic acid,
PMA) the form of the aqueous solution, its amount are equivalent to molybdenum of the addition relative to moisture-free coal charging between 50wppm and 2%.
In slurry mixing tanks 26, arrived with the mixing speed stirring inclusion about 10 defined by rule of thumb according to slurry rheological property
100 minutes and preferably 20 to 60 minutes.By controlling nominal 650 ℉+cut 2 from APS 16, VPS bottoms
The VGO of slurry mixing tanks relative quantity is just being fed to, slurry mixing tanks operation temperature is set.Typical operating temperature arrives 500
In the range of 700 ℉ (260 to 371 DEG C), and more preferably about 600 ℉ (316 DEG C).Slurry containing catalyst mixes from slurry
Close groove and be transported to mashing pump 29.The selection of appropriate mixing condition is the rheological characteristic based on the particular slurry admixture for quantifying just handling
The experimental work of matter.
In the illustrated embodiment, slurry leaves mixing channel 26 under about 600 ℉ (316 DEG C).It is residual to be attributed to hot bottom
Stay thing to be fed to mixing channel 26, and drive away most of residual moisture in the coal in the mixing channel.Such moisture and volatile matter
It is sent to separation unit.The coal stayed in the slurry of slurry mixing tanks 26 has about 0.1 to 1.0% moisture.
Coal slurry and pressure rise are pumped to about 2000 to 3000psig from mixing channel 26 by slurry pumping system 29
(138 arrive 206kg/cm2g).Gained high-pressure slurry mixes with preheating hydrogen-rich processing gas.Also, must in heat exchanger 23
Hydrogen processing gas is preheated when wanting in preheating furnace 27.For extra duty of the heat of hydrogen exchanger from heat separator 9.Heat
Exchanger 11 can be air or water-cooled exchanger.
(138 arrive in about 660 to 700 ℉ (349 to 371 DEG C) and 2000 to 3000psig for coal slurry and hydrogen mixture
206kg/cm2G) input 5 for the first order for being connected in series liquefying reactor 6 is fed under.6 upper tubular container of reactor,
The total length of three reactors is 50 to 250 feet.Because highly exothermic Coal liquefaction causes temperature from a reactor grade
It is raised to next reactor grade.It is excellent in order to maintain the maximum temperature in every one-level to be below about 800 to 900 ℉ (427 to 482 DEG C)
Selection of land injects additional hydrogen processing gas 7 between reactor grade.Hydrogen dividing potential drop in per one-level is preferably maintained at about 1000 and arrived
(69 arrive 138kg/cm to 2000psig2G) at minimum.
The effluent of afterbody from liquefying reactor 6 is fed to heat separator 9, in the heat separator, institute
State effluent and be separated into gas stream and liquid/solid stream.Gas stream is sent to heat exchanger 23, wherein the heat exchanger and hydrogen
Steam stove 27 is just fed to the hydrogen of liquefying reactor 6 to preheat together.Liquid/solid flowing pressure drop from heat separator 9
It is low and APS 16 is fed to by feeding line 14.Gas stream from heat separator 9 after by heat exchanger 23,
Cooled down in heat exchanger 11 and be fed to cold separator 12 to be condensed out naphtha, distillate and the liquid vaporses of solvent, and
And handled to remove H2S and CO2.The major part of next self cooling separator 12 is remaining to be sent next to hydrogen through processing gas
Recovery system 21 by conventional equipment further to be handled, and so as to reclaim the hydrogen wherein contained, the hydrogen then passes through heat
Exchanger 23 and hydrogen furnace 27 are recycled to be mixed with coal slurry.The remainder through processing gas is removed, prevents light fraction heap
Product is in recirculation loop.The hydrogen of recovery can use in system is promoted to a higher rank in downstream hydrogenation processing.Supplement is added on pipeline 22
Hydrogen is to maintain hydrogen dividing potential drop enough in liquefying reactor.
Depressurized liquid/the efflux of solids and hydro carbons condensed during gas cooling is sent to APS 16, is separated in the APS
Into light fraction, naphtha, distillate and bottoms cut.Handle the light fraction and can be used for fuel gas and other to reclaim
The hydrogen and C of purpose1-C4Hydro carbons.Naphtha described in hydrotreating is so that alkadienes and other reactive hydrocarbon compound saturations.
Hydrotreating and 160 ℉+cut of naphtha can be re-formed by catalysis to produce gasoline.Can hydrotreating distillate evaporate
Point, produce the product such as diesel oil and jet fuel.600 to 700 ℉+(316 to 371 DEG C+) (nominally, 650 ℉+(343 DEG C
+)) part of cut is recycled to slurry mixing tanks 26 on pipeline 2.600 to 700 ℉-(316 to 371 DEG C -) are (nominally,
650 ℉-(343 DEG C+)) light fraction, naphtha and distillate cut leave APS on the pipeline of pipeline 15 is schematically indicated as
16。
VPS 28 is fed to from remaining nominal 650 ℉ caused by atmospheric fractionator 16+(343 DEG C+) cut, described
Nominal 650 to 950/1100 ℉ (343 to 510/593 DEG C) VGO cuts and 950/1100 ℉+(510/593 DEG C are separated into VPS
+) bottoms cut (nominally 650 to 1000 ℉ (343 to 538 DEG C) and 1000 ℉+(538 DEG C+) cut).In pipeline 17
At least a portion of upper VGO cuts is added to nominal 650 ℉+(343 DEG C+) streams that slurry mixing tanks 26 are recycled to from APS.Take
Slurry mixing tanks certainly can be transmitted in the pit ash content just handled, a part for the bottoms cut from VPS 28
26, for being recycled to the first order of liquefying reactor 6.This has advantages below：Become entrained in such recycling bottom residual
Catalyst in thing and then also it is recycled to reactor 6.Some or all of VPS bottoms are sent on pipeline 18,
To remove ash content from system, and to produce hydrogen, for road pavement, or the fuel as cement plant.
APS 16 is preferably operated under sufficiently high pressure so that the part of nominal 650 ℉+(343 DEG C+) cut can be
Slurry mixing tanks 26 are recycled in the case of without pumping.
Also the added hydrogen for the technique can be produced by the steam reformation of natural gas or by coal gasification.
Example 1
This example is the present invention to following computer simulation：In 800 ℉ equivalent isothermal temperature (equivalent
Isothermal temperature, EIT) under liquefy bituminous coal, and be fed to the chargings of slurry mixing tanks by 2/1 weight than
650 ℉+/ dry feed coal composition.The cooling that cold hydrogen processing gas is used between liquefying reactor.To the charging of slurry mixing tanks
Comprising through dry coal, 650 ℉+(343 DEG C+) bottoms and VGO from VPS.Gained mixing temperature is 611 ℉
In order that liquefaction inlet temperature is increased to 660 ℉ minimum value, it is necessary to a small amount of extra heat from hydrogen preheating furnace
Amount.It is to reach this coal and degree of switching to stove in the normal operation period that rise condensing temperature or 650 ℉+recirculation rate, which will eliminate,
Needs.
Because the height of the catalyst recycled present in reactor in supplement catalyst and APS bottoms is living
Property dispersed catalyst, the ℉ of preheating temperature 660 are enough to start liquefaction reaction.In this example, added between liquefying reactor cold
Hydrogen processing gas (120 ℉), 820 ℉ are limited to by maximum temperature of reactor.By adding less cold hydrogen processing gas, having can
Higher temperature of reactor (EIT) can be reached.
Example 2
This example is the present invention to following computer simulation：In 800 ℉ equivalent isothermal temperature (equivalent
Isothermal temperature, EIT) under liquefy bituminous coal, and to slurry mixing tanks charging by 3/1 weight than 650 ℉
+/dry feed coal forms.The cooling that cold 650/1000 ℉ VGO from vacuum (distilling) column are used between liquefying reactor.
To slurry mixing tanks charging comprising through dry coal, 650 ℉+bottoms and VGO from VPS.Gained
Mixing temperature is 615 ℉.
Due to the ratio of higher temperature in slurry mixing tanks and increased hydrogen processing gas, (in porch, addition is generally used for
The processing gas of quenching), do not need hydrogen furnace to preheat for this coal and coal degree of switching in the normal operation period.
In this example, using the cold VGO of the extra duty from VPS.The cold hydrogen for replacing using in example 1 using VGO
Processing gas.In this example, maximum temperature of reactor is also limited to 820 ℉.
Example 3
In the one or two example, average condensing temperature (average liquefaction temperature, EIT)
800 ℉ are used to model.This requires high recycling processing gas or the rise of 650/1000 ℉ rate limits temperature.Higher liquefaction temperature
The demand to hydrogen furnace will be further reduced in operation under degree.
Claims (13)
1. a kind of equipment for being used to the charging of solid carbon-containing material containing coal being converted into Canada liquid fuels, including：
A. direct coal liquefaction DCL reactors, the direct coal liquefaction DCL reactors are used for solvent and catalyst being present
Under directly change at high temperature and pressure such solid carbon-containing material for generate hydrocarbon products；
B. atmospheric fractionator, the atmospheric fractionator evaporate for the hydrocarbon products of the DCL reactors to be separated into different boiling
Point, include nominal 650 ℉+(343 DEG C+) cut；
C. vacuum fractionater, the vacuum fractionater are used for one of 650 ℉+cut from the atmospheric fractionator
It is separated into nominal 650 ℉ to 1000 ℉ (343 DEG C to 538 DEG C) and nominal 1000 ℉+(538 DEG C+) cut；
D. slurry mixing tanks, the slurry mixing tanks are used for the part and described 1000 for making 650 ℉+(343 DEG C+) cut
At least a portion of ℉-(538 DEG C -) cut mixes with the solid carbon-containing material containing feed coal, to form slurry；
E. pump, the pump are used for the input that the slurry generated in the slurry mixing tanks is fed to the direct liquefaction reactor
End, except the heating occurred in the liquefying reactor, substantially it is not required to heat the institute that the liquefying reactor generates in addition
State the part of slurry；And
F. heat exchanger, the heat exchanger are just being fed to the input of the direct liquefaction reactor for preheating
Hydrogen, so as to just be fed to the slurry of combination of the input of the direct liquefaction reactor and the temperature of hydrogen is increased to
At least about 660 ℉.
2. equipment according to claim 1, wherein the catalyst includes dispersed molybdenum.
3. equipment according to claim 2, wherein the heat exchanger is described direct comprising being just fed to for preheating
The hydrogen preheating furnace of the hydrogen of the input of liquefying reactor.
4. equipment according to claim 2, wherein the heat exchanger fully heats the hydrogen, so as to just be fed to institute
The temperature of the slurry and hydrogen of stating the combination of the input of direct liquefaction reactor is increased between 660 Hes
Between 700 ℉ (349 and 371 DEG C).
5. equipment according to claim 1, wherein the liquefying reactor includes multiple reactor grades being connected in series, and
And it is additionally contained in and the part of 650 ℉ to 1000 ℉ (343 DEG C to 538 DEG C) cut is fed between the reactor grade enters
Row quenching.
6. a kind of method for solid carbon-containing material containing coal to be converted into liquid fuel, comprise the following steps：
A. in direct liquefaction reactor, directly changed at high temperature and pressure in the case where solvent and catalyst be present such
Solid carbon-containing material is for generation hydrocarbon products；
B. such hydrocarbon products is separated into different boiling cut, includes nominal 650 ℉+(343 DEG C+) cut；
C. by the part of 650 ℉+(343 DEG C+) cut be separated into nominal 650 ℉ to 1000 ℉ (343 DEG C to 538 DEG C) and
1000 ℉+(538 DEG C+) cut；
D. make the part of 650 ℉+(343 DEG C+) cut and at least a portion of 1000 ℉-(538 DEG C -) cut with
The solid carbon-containing material mixing, to form slurry；
E. the input by the slurry pumping to the direct liquefaction reactor, it is being fed to the input of the reactor
Before end, except the heating occurred in the liquefying reactor, substantially it is not required to heat the liquefying reactor generation in addition
The slurry part；And
F. combine the slurry of the pumping and be heated to the hydrogen of a temperature, the temperature just to be fed to the direct liquid
The slurry of the combination and the temperature of hydrogen for changing the input of reactor reach at least about 660 ℉ (349 DEG C).
7. according to the method for claim 6, wherein the catalyst includes dispersed molybdenum.
8. according to the method for claim 7, wherein the effluent from the direct liquefaction reactor is separated into gas stream
With liquid/solid stream, and additionally comprise and the liquefaction reaction is just fed to heat by the heat exchange with the gas stream
The hydrogen of the input of device.
9. according to the method for claim 7, included in stove, heating is just being fed to described in the liquefying reactor in addition
The hydrogen of input.
10. according to the method for claim 7, wherein the catalyst feeds original in the liquefying reactor by phosphomolybdic acid
Position is formed.
11. according to the method for claim 6, wherein the direct liquefaction reactor includes three or more levels series connection company
The adiabatic slurry reactor connect, and additionally comprise by providing hydrogen quenching between the reactor grade described anti-to control
Answer the temperature of device level.
12. according to the method for claim 7, wherein being just fed to the institute of the input of the direct liquefaction reactor
The slurry of combination and the temperature of hydrogen are stated between 660 and 700 ℉ (349 and 371 DEG C).
13. according to the method for claim 7, wherein the reactor includes multiple reactor grades being connected in series, and
It is additionally contained in the part progress that 650 ℉ to 1000 ℉ (343 DEG C to 538 DEG C) cut is fed between the reactor grade
Quenching.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201562165993P | 2015-05-24 | 2015-05-24 | |
| US201562165991P | 2015-05-24 | 2015-05-24 | |
| US62/165,993 | 2015-05-24 | ||
| US62/165,991 | 2015-05-24 | ||
| PCT/US2016/033815 WO2016191387A1 (en) | 2015-05-24 | 2016-05-23 | Direct coal liquefaction process and system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107849460A true CN107849460A (en) | 2018-03-27 |
| CN107849460B CN107849460B (en) | 2021-05-11 |
Family
ID=57393665
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201680040816.4A Expired - Fee Related CN107849460B (en) | 2015-05-24 | 2016-05-23 | Direct coal liquefaction process and system |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN107849460B (en) |
| WO (1) | WO2016191387A1 (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103555357A (en) * | 2013-11-04 | 2014-02-05 | 华东理工大学 | Method for liquifying coal mildly |
| US20140262965A1 (en) * | 2013-03-14 | 2014-09-18 | Accelergy Corporation | Liquid Fuel Production Process and Apparatus Employing Direct and Indirect Coal Liquefaction |
| CN104419438A (en) * | 2013-08-29 | 2015-03-18 | 任相坤 | Direct liquefaction process of coal mixed with medium and low temperature coal tar |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2220193A1 (en) * | 2007-11-16 | 2010-08-25 | Accelergy Shanghai R & D Center Co., Ltd. | Integrated coal-to-liquids process |
| WO2014110085A1 (en) * | 2013-01-14 | 2014-07-17 | Accelergy Corporation | Direct coal liquefaction process |
| US20140296595A1 (en) * | 2013-04-02 | 2014-10-02 | Accelergy Corporation | Methods And Apparatus For Producing Aromatics From Coal |
-
2016
- 2016-05-23 CN CN201680040816.4A patent/CN107849460B/en not_active Expired - Fee Related
- 2016-05-23 WO PCT/US2016/033815 patent/WO2016191387A1/en active Application Filing
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20140262965A1 (en) * | 2013-03-14 | 2014-09-18 | Accelergy Corporation | Liquid Fuel Production Process and Apparatus Employing Direct and Indirect Coal Liquefaction |
| CN104419438A (en) * | 2013-08-29 | 2015-03-18 | 任相坤 | Direct liquefaction process of coal mixed with medium and low temperature coal tar |
| CN103555357A (en) * | 2013-11-04 | 2014-02-05 | 华东理工大学 | Method for liquifying coal mildly |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107849460B (en) | 2021-05-11 |
| WO2016191387A1 (en) | 2016-12-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8585891B2 (en) | Extraction and upgrading of bitumen from oil sands | |
| CN106701178B (en) | A kind of coal tar suspension bed method for hydrogen cracking | |
| CN101429456B (en) | Delay coking hydrogenation combined process for coal oil | |
| JPH0819420B2 (en) | Degradation method for low-grade raw materials | |
| CN102220165A (en) | Process for delaying coking | |
| CN102057018A (en) | Process and apparatus for cooling liquid bottoms from vapor-liquid separator by heat exchange with feedstock during steam cracking of hydrocarbon feedstocks | |
| US11046893B2 (en) | Process and a system for hydrocarbon steam cracking | |
| CN104877707B (en) | The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization | |
| CN104937077A (en) | Direct coal liquefaction process | |
| CN205152158U (en) | Coal tar suspension bed hydrocracking unit | |
| CN102220166A (en) | Delayed coking method | |
| CN105441128B (en) | The temperature control method and its design method and purposes of a kind of hydrogenation technique | |
| US20200165531A1 (en) | Upgrading oil using supercritical fluids | |
| CA1210723A (en) | Two-stage coal liquefaction process | |
| CN107849460A (en) | Direct coal liquefaction technique and system | |
| EP1436362B2 (en) | Hydrodesulfurisation method comprising a stripping section and a vacuum fractionation section | |
| CN104531211B (en) | A kind of coal tar hydrogenating produces technique and the process matched therewith system of fuel or industrial oil | |
| US9994778B2 (en) | Direct coal liquefaction process and system | |
| US20140296595A1 (en) | Methods And Apparatus For Producing Aromatics From Coal | |
| US20170321125A1 (en) | Direct coal liquefaction process | |
| JPH0456873B2 (en) | ||
| US20160340591A1 (en) | Integrated direct coal liquefaction process and system | |
| RU2795466C1 (en) | Unit for the production of needle or anode coke by delayed coking | |
| US11859141B2 (en) | Integrated desolidification for solid-containing residues | |
| US20150191657A1 (en) | Direct coal liquefaction process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210415 Address after: 22 Church Street, liberty corner, New Jersey, USA Applicant after: C2xx Co. Address before: Houston, Texas, USA Applicant before: Yashen Technology |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20210511 |