CN104531187A - Method for preparing tar, coal gas and semi-coke by virtue of pyrolysis of bituminous coal - Google Patents
Method for preparing tar, coal gas and semi-coke by virtue of pyrolysis of bituminous coal Download PDFInfo
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- CN104531187A CN104531187A CN201410836423.7A CN201410836423A CN104531187A CN 104531187 A CN104531187 A CN 104531187A CN 201410836423 A CN201410836423 A CN 201410836423A CN 104531187 A CN104531187 A CN 104531187A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/02—Multi-step carbonising or coking processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
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Abstract
The invention discloses a method for preparing tar, coal gas and semi-coke by virtue of pyrolysis of low-rank coal. The method comprises the following steps of processing pulverized raw material coal as in a three-stage manner, namely, a screening drying stage as the first stage, a low-temperature pyrolysis stage as the second stage and a medium-temperature pyrolysis stage as the third stage, wherein in the first stage, most moisture in the raw material coal is removed, the pulverized coal having the size of below 1mm is screened by wind power and used as a combustion raw material of a three-waste furnace for providing a heat source for a system, dust having the size of below 50 microns in the system is almost removed so that the pre-dust removal effect is achieved and the content of the dust in the end product coal tar is greatly reduced; during the second stage, the reaction temperature is controlled to be about 550-570 DEG C, and thus the highest tar yield is ensured; during the third stage, the reaction temperature is controlled to be about 690-710 DEG C the yield of the coal gas is increased. The products have the advantages of good quality, high yield, energy conservation and environment friendliness and the method has good economic and social benefits and is worthy in popularization and application.
Description
Technical field
The invention belongs to coal chemical technology, relate to a kind of method for upgrading coal pyrolysis, particularly a kind of method being produced semicoke, burnt oil and gas by low-rank coal pyrolysis.
Background technology
Lower-grade metamorphic bituminous, have the features such as moisture is high, volatile matter is high, thermal value is low, its rich reserves, but directly combustion power generation thermo-efficiency is low, how efficiency utilization low-rank coal resource becomes the emphasis of R and D gradually.Pyrolysis (destructive distillation) technology is a kind of conventional Coal dressing technology, and since the last century, domestic and international experts and scholars are the kinds of processes for pyrolysis of coal technological development.
The main representative of external vertical interior hot gas retort is Lu Qi-Si Pierre Gai Si (L-S) low-temperature pyrolysis stove, and this technique is the exploitation of German Lurqi GmbH company, uses gaseous heat-carrier internal heat type vertical continuous stove.Feature is that process structure is simple, invests little, but for making the bed of material have enough ventilation properties, can only use granularity be the lump coal of 20 ~ 80mm as raw material, after broken, smalls is not used, and the utilization ratio of raw material is low; Dry and that retort process is used gaseous heat-carrier is flue gas simultaneously, has been mixed into noble gas component, has caused discharged producer gas calorific value low, is difficult to meet industry and civilian requirement, causes tremendous influence to follow-up further processing and utilization.
U.S. FMC (Food Machinery Corporation) develops COED pyrolytic process, by the multistage pyrolysis of coal, to effectively obtaining coal gas, tar and semicoke.This technique adopts fluid bed powder coal pyrolysis, and point four sections of cascade raising temperatures, all pyrolytic processs all carry out under the atmosphere of anaerobic, improve the yield of oil gas.But technical process is complicated, its hop count is more, during running operation, take into account the discharge etc. of the design temperature of each section of fluidisation pyrolysis oven, pressure, fluidized state and semicoke, controls difficulty large.Large owing to adopting fluidized bed gas to carry Dust Capacity secretly, follow-up system easily blocks, and containing a lot of particulate semicoke in tar, also needs to be removed.
The object of the present invention is to provide a kind of method for upgrading coal pyrolysis, in order to solve the problems such as the heat utilization efficiency existed in original technology is low, hydrocarbon yield is low, Dust Capacity is large.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of method for upgrading coal pyrolysis reducing coal tar dustiness, improve tar and gas yield.
The technical solution adopted for the present invention to solve the technical problems is: the method being produced tar, coal gas and semicoke by bituminous coal pyrolysis, comprises the steps:
A, the feed coal of granularity≤30mm is sent into screening dryer section, feed coal by heat smoke heat drying, and utilizes heat smoke to carry out wind filter to feed coal, and the coal dust of below granularity 1mm is sent into coal dust classifier by heat smoke and is separated;
B, the feed coal dried granularity of screening being greater than 1mm send into low temperature pyrogenation section, and feed coal is heated to 540 ~ 570 DEG C by external source, feed coal generation pyrolysis Heat of Formation semicoke solid product and a large amount of tar steam and a small amount of coal gas;
C, hot semicoke solid product low temperature pyrogenation section generated send into medium temperature carbonization section, and hot semicoke solid product is heated to 680 ~ 720 DEG C by external source, and hot semicoke solid product continues pyrolysis Heat of Formation semicoke and a large amount of coal gas and a small amount of tar steam;
D, hot semicoke medium temperature carbonization section generated send into device for generating power by waste heat, and obtain finished product semicoke after hot semicoke cooling, the sensible heat of hot semicoke is recovered and is converted into electric energy simultaneously;
E, tar steam low temperature pyrogenation section and medium temperature carbonization section generated and coal gas send into purification upgrading workshop section, after purifying, cool, being separated, obtain finished product tar and purified gas.
Wherein, in aforesaid method step a, the coal dust of below granularity 1mm is separated by heat smoke feeding coal dust classifier, and the coal dust of separation is sent in three wastes stove and burnt; Meanwhile, step e purification upgrading workshop section produces coke powder, concentrated waste water and ammonia-contaminated gas are also sent in three wastes stove and are burnt; The high-temperature flue gas produced that burns in three wastes stove sends into medium temperature carbonization section, low temperature pyrogenation section, screening dryer section successively as thermal source.
Wherein, in aforesaid method step a, the coal dust of below granularity 1mm is separated by heat smoke feeding coal dust classifier, the heat smoke be separated sends into regenerative apparatus, is sent into condensation water collector, recycle after the water vapour in flue gas is condensed in regenerative apparatus by after cold flue gas cooling; The cold flue gas that condensation water collector is discharged, as the low-temperature receiver of regenerative apparatus, is discharged by heating rear section, and part feeding three wastes stove uses as circulating flue gas.
Wherein, in aforesaid method step a, feed coal by heat smoke heat drying to moisture 3 ~ 5% (mass content).
Wherein, in aforesaid method step b, feed coal is heated to 550 ~ 570 DEG C by external source.
Wherein, in aforesaid method step c, hot semicoke solid product is heated to 690 ~ 710 DEG C by external source.
Wherein, in aforesaid method step b, the time that low temperature pyrogenation section carries out low temperature pyrogenation is 35 ~ 40 minutes; In step c, the time that medium temperature carbonization section carries out medium temperature carbonization is 14 ~ 16 minutes.
Wherein, in aforesaid method, described feed coal is at least one in long-flame coal, non-caking coal, weakly caking coal.
Wherein, low temperature pyrogenation section and medium temperature carbonization section can be arranged in same rotary kiln.
The invention has the beneficial effects as follows: contriver finds, by feed coal about 550 ~ 570 DEG C pyrolysis, can produce a large amount of tar steam, improve tar yield fully, and can produce a large amount of coal gas at about 690 ~ 710 DEG C, improve gas yield fully; The dust of less than 10 microns has a strong impact on the quality of terminal tar products simultaneously.Therefore, raw material coal dust of the present invention divides three sections to process by applicant, first paragraph is screening dryer section, in this stage feed coal, most of moisture is removed, select the coal dust of below 1mm as three wastes stove combustion material through air sifting, for system provides thermal source, so less than 50 microns dust are almost completely removed in present system simultaneously, serve the effect of pre-dedusting, greatly reduce the dustiness of end product coal tar.Second segment is low temperature pyrogenation section, temperature of reaction is controlled at about 550 ~ 570 DEG C, ensures the highest tar yield.3rd section is medium temperature carbonization section, temperature of reaction is controlled at about 690 ~ 710 DEG C, to increase gas yield.Pyrolysis is divided two sections in this technique to carry out, gaseous product segmentation extracts, and temperature individually controls, and ensures that raw material oil yield rate in second segment optimal temperature maximizes, increases gas yield further simultaneously after the 3rd section of raised temperature.
Three wastes stove is used to provide thermal source for reactive system in present invention process, and raw material be separate in production process coal dust, coke powder, improve raw material availability, simultaneously with the concentrated waste water, the waste gas that produce in the mode treatment and purification grading process of high temperature incineration, decrease three-protection design cost, there is the feature of energy-saving high-efficiency environment-friendly.
Present invention process comprises afterheat generating system, adopts solid direct heat exchange boiler, is sent into by high-temperature hot semicoke in device for generating power by waste heat, while cooling semicoke, again semicoke sensible heat is converted into electric energy and exports, improve whole system capacity usage ratio.
Backheat and condensation water collector is also comprised in present invention process, raw coal drying process overwhelming majority moisture enters in heat smoke, and directly discharge causes the wasting of resources, this device act as the moisture collected by condensation in flue gas, recycled, improve the utilization ratio of resource.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the present invention's wherein a kind of embodiment.
Embodiment
Below in conjunction with drawings and Examples, the present invention is further described.
The present invention produces the method for tar, coal gas and semicoke by bituminous coal pyrolysis, comprises the steps:
A) feed coal of granularity≤30mm is sent into screening dryer section, in this stage, feed coal, by heat smoke heat drying, is dried to moisture 3 ~ 5%; Carry out wind filter to raw coal, the coal dust of below 1mm is carried to coal dust moisture eliminator by flue gas simultaneously, and effectively reduce the dustiness of purification upgrading workshop section raw gas, make tar quality-improving, the cycle of operation increases; Screening dryer section, by adjustment ventilation flow rate, can obtain the coal dust of different content, and as the main fuel of three wastes stove, native system normally runs no longer needs pulverized coal preparation system, has saved the energy consumption of pulverized coal preparation system;
B) dried feed coal will be sieved and send into low temperature pyrogenation section by sealing screw feeder, in this stage, raw material is heated to about 550 ~ 570 DEG C by external source, in the process pyrolysis occurs, main Heat of Formation semicoke and a large amount of tar steam, produce a small amount of coal gas simultaneously;
C) low temperature pyrogenation section solid product is sent into medium temperature carbonization section, in this stage, heating final temperature controls at about 690 ~ 710 DEG C, and solid material continues pyrolysis, generates a large amount of coal gas, produces a small amount of tar simultaneously;
D) hot for medium temperature carbonization section solid phase prod semicoke is sent into device for generating power by waste heat, obtain finished product semicoke after semicoke cooling, the sensible heat of semicoke is converted into electric energy by efficient recovery simultaneously;
E) coal gas of low temperature pyrogenation section and medium temperature carbonization section, tar steam are sent into purification upgrading workshop section, through purification, cooling, be separated after obtain finished product tar and pure qi (oxygen);
The inventive method is further comprising the steps of:
F) coal dust that screening dryer section outlet heat smoke carries is sent in three wastes stove and is burnt after coal dust classifier is separated, and by the coke powder produced in purification upgrading workshop section, concentrates waste water and contains NH
3waste gas is sent in three wastes stove and is burnt, and three wastes stove carries out burning disposal to waste water,waste gas and industrial residue at about 1700 DEG C temperature, and the high-temperature flue gas that burning produces sends into medium temperature carbonization section, low temperature pyrogenation section, screening dryer section successively as thermal source after temperature adjustment;
G) waste gas sends into regenerative apparatus after coal dust classifier removing dust, to enter after being cooled by cold flue gas in regenerative apparatus condensation water collector, in flue gas, water vapour reclaims for plant area after condensation, cooled flue gas comes back to 8-regenerative apparatus as low-temperature receiver, discharged by heating rear section, part uses as circulating flue gas.
Below by embodiment, the specific embodiment of the invention is described further, but not therefore by protection scope of the present invention restriction in one embodiment.
Embodiment one
Embodiment feed coal is long-flame coal, and feedstock analysis data are as shown in table 1:
Table 1 feedstock analysis table
A, the feed coal of granularity≤30mm is sent into screening dryer section, feed coal to moisture 4%, and is utilized heat smoke to carry out wind filter to feed coal by heat smoke heat drying, and the coal dust of below granularity 1mm is sent into coal dust classifier by heat smoke and is separated.
B, the feed coal dried granularity of screening being greater than 1mm send into low temperature pyrogenation section, and feed coal is heated to about 560 DEG C by external source, feed coal generation pyrolysis Heat of Formation semicoke solid product and a large amount of tar steam and a small amount of coal gas; The time of low temperature pyrogenation is 38 minutes.
C, hot semicoke solid product low temperature pyrogenation section generated send into medium temperature carbonization section, and hot semicoke solid product is heated to about 700 DEG C by external source, and hot semicoke solid product continues pyrolysis Heat of Formation semicoke and a large amount of coal gas and a small amount of tar steam; The time of medium temperature carbonization is 15 minutes.
D, hot semicoke medium temperature carbonization section generated send into device for generating power by waste heat, and obtain finished product semicoke after hot semicoke cooling, the sensible heat of hot semicoke is recovered and is converted into electric energy simultaneously.
E, tar steam low temperature pyrogenation section and medium temperature carbonization section generated and coal gas send into purification upgrading workshop section, after purifying, cool, being separated, obtain finished product tar and purified gas.
In f, step a, the coal dust of below granularity 1mm is separated by heat smoke feeding coal dust classifier, and the coal dust of separation is sent in three wastes stove and burnt; Meanwhile, step e purification upgrading workshop section produces coke powder, concentrated waste water and ammonia-contaminated gas are also sent in three wastes stove and are burnt; The high-temperature flue gas (1700 DEG C) produced that burns in three wastes stove sends into medium temperature carbonization section, low temperature pyrogenation section, screening dryer section successively as thermal source after temperature adjustment.
In g, step a, the coal dust of below granularity 1mm is separated by heat smoke feeding coal dust classifier, and the heat smoke of separation sends into regenerative apparatus, in regenerative apparatus, sent into condensation water collector by after cold flue gas cooling, recycling after the water vapour in flue gas is condensed; The cold flue gas that condensation water collector is discharged, as the energy of regenerative apparatus, is discharged by heating rear section, and part feeding three wastes stove uses as circulating flue gas.
Pyrolysis product main condition are in table 2:
Table 2 pyrolysis product situation
In usual production operation, tar yield only can reach about 75% of lattice gold experimental value, and this device measured result can bring up to 94.86%, and the productive rate of coal gas is also increased to 115.04% simultaneously.
Claims (8)
1. produced the method for tar, coal gas and semicoke by bituminous coal pyrolysis, it is characterized in that comprising the steps:
A, the feed coal of granularity≤30mm is sent into screening dryer section, feed coal by heat smoke heat drying, and utilizes heat smoke to carry out wind filter to feed coal, and the coal dust of below granularity 1mm is sent into coal dust classifier by heat smoke and is separated;
B, the feed coal dried granularity of screening being greater than 1mm send into low temperature pyrogenation section, and feed coal is heated to 540 ~ 570 DEG C by external source, feed coal generation pyrolysis Heat of Formation semicoke solid product and a large amount of tar steam and a small amount of coal gas;
C, hot semicoke solid product low temperature pyrogenation section generated send into medium temperature carbonization section, and hot semicoke solid product is heated to 680 ~ 720 DEG C by external source, and hot semicoke solid product continues pyrolysis Heat of Formation semicoke and a large amount of coal gas and a small amount of tar steam;
D, hot semicoke medium temperature carbonization section generated send into device for generating power by waste heat, and obtain finished product semicoke after hot semicoke cooling, the sensible heat of hot semicoke is recovered and is converted into electric energy simultaneously;
E, tar steam low temperature pyrogenation section and medium temperature carbonization section generated and coal gas send into purification upgrading workshop section, after purifying, cool, being separated, obtain finished product tar and purified gas.
2. the method being produced tar, coal gas and semicoke by bituminous coal pyrolysis according to claim 1, is characterized in that: in step a, the coal dust of below granularity 1mm is separated by heat smoke feeding coal dust classifier, and the coal dust of separation is sent in three wastes stove and burnt; Meanwhile, step e purification upgrading workshop section produces coke powder, concentrated waste water and ammonia-contaminated gas are also sent in three wastes stove and are burnt; The high-temperature flue gas produced that burns in three wastes stove sends into medium temperature carbonization section, low temperature pyrogenation section, screening dryer section successively as thermal source.
3. the method being produced tar, coal gas and semicoke by bituminous coal pyrolysis according to claim 1 and 2, it is characterized in that: in step a, the coal dust of below granularity 1mm is separated by heat smoke feeding coal dust classifier, the heat smoke be separated sends into regenerative apparatus, in regenerative apparatus, sent into condensation water collector by after cold flue gas cooling, recycle after the water vapour in flue gas is condensed; The cold flue gas that condensation water collector is discharged, as the low-temperature receiver of regenerative apparatus, is discharged by heating rear section, and part feeding three wastes stove uses as circulating flue gas.
4. the method being produced tar, coal gas and semicoke by bituminous coal pyrolysis according to claim 1,2 or 3, is characterized in that: in step a, feed coal by heat smoke heat drying to moisture 3 ~ 5%.
5. the method being produced tar, coal gas and semicoke by bituminous coal pyrolysis according to claim 1,2 or 3, it is characterized in that: in step b, feed coal is heated to 550 ~ 570 DEG C by external source.
6. the method being produced tar, coal gas and semicoke by bituminous coal pyrolysis according to claim 1,2 or 3, is characterized in that: in step c, hot semicoke solid product is heated to 690 ~ 710 DEG C by external source.
7. the method being produced tar, coal gas and semicoke by bituminous coal pyrolysis according to claim 1,2 or 3, is characterized in that: in step b, and the time that low temperature pyrogenation section carries out low temperature pyrogenation is 35 ~ 40 minutes; In step c, the time that medium temperature carbonization section carries out medium temperature carbonization is 14 ~ 16 minutes.
8. the method being produced tar, coal gas and semicoke by bituminous coal pyrolysis according to claim 1,2 or 3, is characterized in that: described feed coal is at least one in long-flame coal, non-caking coal, weakly caking coal.
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| CN104862027A (en) * | 2015-04-28 | 2015-08-26 | 袁继海 | Method and device for combined drying and carbonizing of lump coal and powdered coal |
| CN105907413A (en) * | 2016-05-04 | 2016-08-31 | 无锡亿恩科技股份有限公司 | Low-temperature carbonization process for low-order pulverized coal |
| CN106513150A (en) * | 2016-12-16 | 2017-03-22 | 北京神雾电力科技有限公司 | Semicoke grinding system and method |
| CN106865659A (en) * | 2017-03-02 | 2017-06-20 | 西安建筑科技大学 | A kind of coal low temperature distillation high temperature in wastewater disposal and Application way |
| CN107033963A (en) * | 2017-05-31 | 2017-08-11 | 河南龙成煤高效技术应用有限公司 | A kind of pyrolytic process of coal device |
| CN108559542A (en) * | 2018-04-11 | 2018-09-21 | 西安交通大学 | Steam predrying and low temperature pyrogenation coupled system and operation method |
| CN110423628A (en) * | 2019-09-09 | 2019-11-08 | 重庆润科新材料技术有限公司 | A kind of low order dry distillation of coal process units and method |
| CN111253973A (en) * | 2018-11-30 | 2020-06-09 | 浙江天禄环境科技有限公司 | Method and system for preparing synthesis gas through gasification reduction |
| CN111253975A (en) * | 2018-11-30 | 2020-06-09 | 浙江天禄环境科技有限公司 | Method for grading and utilizing low-rank coal |
| CN111534311A (en) * | 2020-04-01 | 2020-08-14 | 华北电力大学 | Double-chamber organic solid waste pyrolysis device and method |
| CN115261052A (en) * | 2022-07-05 | 2022-11-01 | 西安科技大学 | Oil-rich coal and magnetic catalyst co-catalytic pyrolysis process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104862027B (en) * | 2015-04-28 | 2017-03-08 | 袁继海 | A kind of lump coal and fine coal combination drying method for destructive distillation and device |
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| CN106513150A (en) * | 2016-12-16 | 2017-03-22 | 北京神雾电力科技有限公司 | Semicoke grinding system and method |
| CN106865659A (en) * | 2017-03-02 | 2017-06-20 | 西安建筑科技大学 | A kind of coal low temperature distillation high temperature in wastewater disposal and Application way |
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| CN108559542B (en) * | 2018-04-11 | 2020-07-28 | 西安交通大学 | Steam pre-drying and low-temperature pyrolysis coupling system and operation method |
| CN108559542A (en) * | 2018-04-11 | 2018-09-21 | 西安交通大学 | Steam predrying and low temperature pyrogenation coupled system and operation method |
| CN111253973A (en) * | 2018-11-30 | 2020-06-09 | 浙江天禄环境科技有限公司 | Method and system for preparing synthesis gas through gasification reduction |
| CN111253975A (en) * | 2018-11-30 | 2020-06-09 | 浙江天禄环境科技有限公司 | Method for grading and utilizing low-rank coal |
| CN110423628A (en) * | 2019-09-09 | 2019-11-08 | 重庆润科新材料技术有限公司 | A kind of low order dry distillation of coal process units and method |
| CN111534311A (en) * | 2020-04-01 | 2020-08-14 | 华北电力大学 | Double-chamber organic solid waste pyrolysis device and method |
| CN111534311B (en) * | 2020-04-01 | 2021-05-18 | 华北电力大学 | Double-chamber organic solid waste pyrolysis device and method |
| CN115261052A (en) * | 2022-07-05 | 2022-11-01 | 西安科技大学 | Oil-rich coal and magnetic catalyst co-catalytic pyrolysis process |
| CN115261052B (en) * | 2022-07-05 | 2023-04-07 | 西安科技大学 | Oil-rich coal and magnetic catalyst co-catalytic pyrolysis process |
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