CN111253977A - Method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal - Google Patents
Method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal Download PDFInfo
- Publication number
- CN111253977A CN111253977A CN201811459025.2A CN201811459025A CN111253977A CN 111253977 A CN111253977 A CN 111253977A CN 201811459025 A CN201811459025 A CN 201811459025A CN 111253977 A CN111253977 A CN 111253977A
- Authority
- CN
- China
- Prior art keywords
- coal
- temperature
- low
- gas
- mixed gas
- 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.)
- Pending
Links
- 239000003245 coal Substances 0.000 title claims abstract description 208
- 238000000034 method Methods 0.000 title claims abstract description 118
- 239000011280 coal tar Substances 0.000 title claims abstract description 48
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 37
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 35
- 239000011286 gas tar Substances 0.000 title claims abstract description 13
- 239000007789 gas Substances 0.000 claims abstract description 171
- 238000002309 gasification Methods 0.000 claims abstract description 114
- 238000011946 reduction process Methods 0.000 claims abstract description 93
- 238000006243 chemical reaction Methods 0.000 claims abstract description 90
- 238000001035 drying Methods 0.000 claims abstract description 89
- 230000008569 process Effects 0.000 claims abstract description 82
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 41
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 41
- 238000002407 reforming Methods 0.000 claims abstract description 35
- 239000000203 mixture Substances 0.000 claims abstract description 33
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 21
- 239000001301 oxygen Substances 0.000 claims abstract description 21
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 15
- 238000000746 purification Methods 0.000 claims abstract description 12
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 239000002893 slag Substances 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 59
- 239000000428 dust Substances 0.000 claims description 25
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 19
- 238000001833 catalytic reforming Methods 0.000 claims description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims description 18
- 239000003054 catalyst Substances 0.000 claims description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 13
- 230000003197 catalytic effect Effects 0.000 claims description 12
- 238000006477 desulfuration reaction Methods 0.000 claims description 12
- 230000023556 desulfurization Effects 0.000 claims description 12
- 238000004519 manufacturing process Methods 0.000 claims description 12
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 11
- 238000007254 oxidation reaction Methods 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 11
- 230000003647 oxidation Effects 0.000 claims description 10
- 235000019476 oil-water mixture Nutrition 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 6
- 230000026676 system process Effects 0.000 claims description 2
- 239000007787 solid Substances 0.000 description 15
- 238000006722 reduction reaction Methods 0.000 description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 11
- 239000003546 flue gas Substances 0.000 description 11
- 238000002485 combustion reaction Methods 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 9
- 239000002994 raw material Substances 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 150000001875 compounds Chemical class 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 238000004880 explosion Methods 0.000 description 7
- 230000014759 maintenance of location Effects 0.000 description 7
- 229910052717 sulfur Inorganic materials 0.000 description 7
- 239000011593 sulfur Substances 0.000 description 7
- 230000007246 mechanism Effects 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 5
- 230000009467 reduction Effects 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 230000009471 action Effects 0.000 description 4
- 238000001599 direct drying Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000011269 tar Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 150000001491 aromatic compounds Chemical class 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 239000010426 asphalt Substances 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 238000004200 deflagration Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000003077 lignite Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 229910052755 nonmetal Inorganic materials 0.000 description 2
- 150000002843 nonmetals Chemical class 0.000 description 2
- 235000019198 oils Nutrition 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 230000000607 poisoning effect Effects 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 229910052703 rhodium Inorganic materials 0.000 description 2
- 229910052707 ruthenium Inorganic materials 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- -1 syngas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Industrial Gases (AREA)
Abstract
The invention relates to a method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal, wherein the low-rank coal is sequentially treated by a drying process and a gasification reduction process to obtain the upgraded coal with temperature and an oil-gas mixture, the upgraded coal with temperature is treated by a cold slag humidifying process to obtain the upgraded coal, the oil-gas mixture is subjected to a purification process to obtain a mixture gas and the coal tar, and the mixture gas contains CO and H2And hydrocarbons, wherein the gasification reduction process is a chemical reaction process for heating the dried low-rank coal under the oxygen-free or micro-oxygen condition, and the gasification reduction process is two-stage; the mixed gas is treated by partial hydrocarbon reforming conversion process to obtain the mixed gas containing CO and H2Of synthesis gas. In the invention, the obtained products have various types, the yield of the coal tar is high, the yield of the synthesis gas is high, the heat value is high, the volatile components in the obtained upgraded coal are less, and the effective resources in the low-rank coal are fully and effectively utilized.
Description
Technical Field
The invention relates to the technical field of clean utilization of coal substances, in particular to a method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal.
Background
More than half of the coal reserves already explored in China are low-rank coals, and the volatile components in the low-rank coals are equivalent to 1000 hundred million tons of oil and gas resources. The low-rank coal mainly has the characteristics of high moisture and high volatility, flame is long and has smoke during combustion, the coalification degree is low, and typical coal types are brown coal and long flame coal. The coal-rich, oil-less and gas-deficient coal in China becomes a major subject of the clean coal technology at present by how to efficiently utilize low-rank coal. However, both combustion power generation and modern coal chemical utilization have extremely low comprehensive utilization efficiency due to the three characteristics of high water content, high ash content and low calorific value.
At present, the utilization mode of low-rank coal is mainly direct combustion or gasification, wherein direct combustion power generation is one of the most common utilization modes, and according to incomplete statistics, more than 90% of lignite in China is used for power station boilers and various industrial boilers. The direct combustion of the low-rank coal not only wastes rich oil and gas resources contained in the coal, has low efficiency, but also pollutes the environment, easily causes a large amount of greenhouse gases such as SOx and NOx, and causes severe weather environments such as acid rain. The modern coal chemical technology uses coal gasification as a technical tap, and primary raw materials CO and H required by chemical synthesis are obtained by gasification2However, the coal gasification technology has not developed to date, and a mature large-scale commercial low-rank coal gasification technology has not yet been formed. In the prior art, low-rank coal gasification is used for preparing CO and H2Generally, low-rank coal is pyrolyzed to obtain raw coal gas and upgraded coal, and the pyrolysis is generally carried out in the presence of a large amount of oxygen (or air), wherein a part of coal is reacted with oxygen to supply heat and generate a large amount of CO2. Due to CO2Can not be combusted, belongs to ineffective gas, and because of aerobic combustion, the nitrogen content in the crude gas is too high, thereby reducing the energy density of the crude gas and reducing the calorific value of the crude gas except for returningBesides the combustion of the furnace, the crude gas produced by pyrolysis has low economic value, and the utilization rate of oil gas resources in coal is low. And CO is generated by burning part of coal and oxygen to supply heat2The quantity of upgraded coal is less, coal resources in low-rank coal are greatly wasted, and no related integrated equipment is available, so that the low-rank coal can be used for continuously producing gas, upgraded and prepared coal tar, and continuous large-scale production can be realized.
Disclosure of Invention
In view of the above, the present invention aims to provide a method for preparing upgraded coal, synthesis gas and coal tar from low-rank coal, wherein the method comprises the steps of preparing oil-gas mixture and solid upgraded coal with temperature by carrying out reduction and classification on dried low-rank coal under an oxygen-free or micro-oxygen condition, cooling and humidifying the upgraded coal with temperature to prepare the upgraded coal with certain moisture and normal temperature, wherein the upgraded coal has few volatile components and high quality; the oil-gas mixture is further processed to obtain coal tar and mixed gas, and the yield of the obtained coal tar is high; reforming and converting the mixed gas to prepare CO and H rich gas2The synthetic gas has high yield and high heat value, the obtained products have various types, and the effective resources in the low-rank coal are fully and effectively utilized.
The invention provides a method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal, which comprises the following steps: the method comprises the steps that low-rank coal is sequentially treated through a drying process and a gasification reduction process to obtain upgraded coal with temperature and an oil-gas mixture, the upgraded coal with temperature is treated through a cold slag humidifying process to obtain upgraded coal, the oil-gas mixture is subjected to a purification process to obtain mixed gas and coal tar, and the mixed gas contains CO and H2And hydrocarbons, wherein the gasification reduction process is a chemical reaction process for heating the dried low-rank coal under the oxygen-free or micro-oxygen condition, and the gasification reduction process is two-stage;
the mixed gas is treated by partial hydrocarbon reforming conversion process to obtain the mixed gas containing CO and H2The synthesis gas of (2).
The drying process removes most of moisture in the low-rank coal to obtain dried low-rank coal and waste gas, and the dried low-rank coalThe coal firstly enters a first-stage gasification reduction process and then enters a second-stage gasification reduction process, the dried low-rank coal reacts in the first-stage gasification reduction process to obtain first-stage gas and first-stage solid, the first-stage solid enters the second-stage gasification reduction process to be continuously gasified to obtain second-stage gas and second-stage solid, the second-stage solid is upgraded coal with temperature, and the first-stage gas and the second-stage gas are both high-temperature oil-gas mixtures. The oxygen-free or micro-oxygen environment adopted by the gasification reduction process is mainly divided into the following conditions: (1) the air carried in the gaps between the raw material low-rank coal and the materials; (2) a small amount of mixed air is leaked from a feed inlet, a discharge outlet and the like of the gasification reduction process; (3) under the explosion limit value, O accounting for 5 percent of the coal by mass can be slightly introduced into the gasification reduction process2Or (air), and further preferably, O in an amount of 3% by mass of the coal is introduced2Or (air), is beneficial to improving the temperature of the gasification reduction reaction, preventing coking and the like, and simultaneously ensures the safety and stability of the whole gasification reduction process reaction; the dried low-rank coal is preferably subjected to gasification reduction reaction in an oxygen-free environment, so that the condition that the dried low-rank coal is subjected to combustion reaction with oxygen in the reaction process of the gasification reduction process to generate a large amount of incombustible CO is avoided2Thereby ensuring CO in the obtained high-temperature oil-gas mixture2The volume percentage is smaller, which is beneficial to the subsequent preparation of the synthesis gas with high energy density, and the process steps are less, simple and easy to operate, so that the reaction can be safely carried out. The high-temperature oil-gas mixture contains CO and H2、CO2The high-temperature oil-gas mixture generated by each stage of gasification reduction process is respectively subjected to purification process to remove dust and recover impurity gases such as coal tar and sulfur-containing compounds, so that coal tar and purified mixed gas are obtained; preferably, mixed gas obtained after purifying the oil-gas mixture after each stage of gasification and reduction is mixed together and then enters a reforming process; the mixed gas mainly contains CO and H2And hydrocarbons, CO and H being well known2Can be directly used as a primary raw material for chemical synthesis, and hydrocarbons can be reformed to generate CO and H2Therefore, part of hydrocarbons in the mixed gas is reformed and converted by the reforming and conversion process to obtain the mixed gas containing CO and H2Of the synthesis gas, CO and H in the synthesis gas2Part of the original CO and H in the mixed gas2The other part is derived from reforming and converting part of the hydrocarbons to obtain a product containing CO and H2Greatly improve CO and H in the synthesis gas2Total volume percent, heating value increased. The method not only can prepare the synthesis gas by adopting various ways, but also can obtain the product coal tar and upgraded coal, and effectively utilizes resources in the low-rank coal by classification and quality.
If the low-rank coal contains a large amount of moisture, the heat consumption in the gasification reduction reaction process is large. The drying medium of the drying process can be flue gas or water vapor, and the drying can be divided into direct drying and indirect drying. When flue gas is used as a drying medium, although the drying efficiency of the flue gas in direct contact with low-rank coal is the highest, the volume percentage of oxygen in the drying process environment is strictly controlled to be below an explosion limit when the flue gas is used for drying so as to prevent deflagration, and the efficiency of flue gas indirect drying is not ideal, so that steam drying is preferred for production safety and drying efficiency. The direct drying of the water vapor may cause the water vapor to react with the low-rank coal to consume resources, so the drying mode of indirectly drying the low-rank coal by the water vapor is adopted to prevent the moisture in the water vapor from entering the low-rank coal. In addition, if the pressure of the steam is too high and the temperature is too high in the drying process, part of volatile matters in the low-rank coal can escape easily in the drying process, on one hand, the escape of the volatile matters can bring potential safety hazards, on the other hand, the gas yield of a subsequent gasification reduction process can be influenced, so that the drying steam pressure in the drying process is not too high, the drying effect can be ensured, and the volatile matters in the low-rank coal can not be gasified.
Therefore, preferably, the drying process adopts water vapor for indirect drying, the pressure of the water vapor is 0.3-1.5Mpa, the temperature of the water vapor is 105-250 ℃, the water content of the outlet material of the drying process is not more than 7 wt%, and the temperature of the outlet material of the drying process is 50-150 ℃.
Further preferably, the drying process adopts water vapor for indirect drying, the pressure of the water vapor is 0.6-1.2Mpa, the temperature of the water vapor is 120-200 ℃, the water content of the outlet material of the drying process is not more than 6 wt%, and the temperature of the outlet material of the drying process is 80-130 ℃.
Wherein, the gasification reduction process can be one-stage or multi-stage. When a first-stage gasification reduction process is adopted, mainly aiming at obtaining most of high-temperature oil-gas mixture, the temperature directly influences the subsequent gas production, the yield of the upgraded coal with temperature and the temperature of the first-stage upgraded coal with temperature, the reaction temperature of the gasification reduction process is 350-800 ℃, the volatile content in the upgraded coal with temperature is 8-15 wt%, and further preferably, the reaction temperature of the gasification reduction process is 400-750 ℃; still more preferably 450-700 ℃. When the multistage gasification reduction process is adopted, the multistage gasification reduction process mainly has the main function of continuously gasifying certain amount of high-boiling-point oily substances (such as similar asphalt and the like) which cannot be gasified in a certain retention time and cannot be separated out or the temperature cannot reach the polycondensation reaction conditions of phenolic compounds, aromatic hydrocarbon compounds and the like in a certain retention time, and continuously reacting and gasifying the solid substances (including gasified pulverized coal, solid impurities and the like) which cannot be gasified in the previous stage gasification reduction process, so that the gas yield and the quality of the upgraded coal with the temperature are improved. Therefore, preferably, the gasification reduction process comprises a primary gasification reduction process and a secondary gasification reduction process, the low-rank coal is sequentially treated by a drying process, the primary gasification reduction process and the secondary gasification reduction process to obtain upgraded coal with temperature and an oil-gas mixture, and the mixed gas contains CO and H2And hydrocarbons. Still further preferably, the feeding temperature of the primary gasification reduction process is 80-120 ℃, the reaction temperature of the primary gasification reduction process is 450-650 ℃, the gas outlet temperature of the primary gasification reduction process is 180-550 ℃, and the discharging temperature of the primary gasification reduction process is 350-600 ℃; the feeding temperature of the secondary gasification reduction process is 350-600 ℃, the reaction temperature of the secondary gasification reduction process is 550-800 ℃, the discharging temperature of the secondary gasification reduction process is 450-750 ℃, and the secondary gasThe gas outlet temperature of the reduction process is 450-700 ℃, under the process conditions, most of volatile components in the dried low-rank coal are completely gasified, the yield and gas amount of an oil-gas mixture are increased, the volatile components in the obtained upgraded coal with temperature are reduced, and the volatile component content in the obtained upgraded coal with temperature is less than 3-8 wt%.
The purification process comprises a dust removal process, a cooling process, an oil-water separation process and a desulfurization process, wherein the oil-gas mixture is sequentially treated by the dust removal process, the cooling process and the desulfurization process to obtain a mixed gas and an oil-water mixture, and the mixed gas contains CO and H2And hydrocarbons, wherein the oil-water mixture is treated by an oil-water separation process to obtain coal tar. The high-temperature oil-gas mixture contains a large amount of dust, coal tar, water vapor, sulfur-containing compounds and the like; firstly, a dust removal process is utilized for removing dust, so that the temperature of an oil-gas mixture is prevented from being reduced in the dust removal process, and coal tar, water vapor and the like are condensed into liquid and adhered with a large amount of dust to cause the blockage of a subsequent process pipeline and the reduction of the dust removal effect; condensing the gas coal tar and water vapor in the oil-gas mixture into a liquid oil-water mixture by using a cooling process, and treating the oil-water mixture by using an oil-water separation process to obtain the coal tar product, wherein the coal tar is brown and has a relative density of about 0.85kg/m3The main components are cyclane, alkane, aromatic compound and the like; and finally, removing sulfur-containing compounds from the residual gas after the cooling process through a desulfurization process, so as to prevent the sulfur-containing compounds from causing catalyst poisoning in the subsequent process.
Preferably, the mixed gas is subjected to a partial hydrocarbon reforming conversion process, so that the components of the gas in the mixed gas are directly reformed and converted into CO and H without separation2Because the reforming conversion is only intended to convert hydrocarbons to CO and H2The mixed gas already contains a part of CO and H2Therefore, there is no need to remove hydrocarbons from the mixtureThe separated body is then reformed and converted into hydrocarbon, and this operation saves technological steps and results in high economic benefit.
Reforming conversion mainly includes partial catalytic oxidation, steam catalytic reforming conversion, and non-catalytic reforming conversion. The catalyst is needed for partial catalytic oxidation and steam catalytic reforming conversion, the catalyst for reforming conversion process is mostly a load type catalyst, and the active components are mainly non-metals such as Ni, Co, Fe, Cu and the like and noble metals such as Rh, Ru, Pt and the like. Reforming conversion generally requires heat supply, and direct heat supply or indirect heat supply can be adopted. CO and H in syngas2The source of the (C) is two parts, one part is CO and H obtained by catalytic conversion of partial hydrocarbons in the mixed gas2The other part is original H in the mixed gas2And CO.
The partial catalytic oxidation adopts oxygen and partial hydrocarbon to burn and directly supply heat, and partial hydrocarbon in the mixed gas reacts with steam to generate CO and H under the action of the catalyst2(ii) a When in steam catalytic reforming conversion, external heat supply is adopted, and partial hydrocarbons in the mixed gas react with steam to generate CO and H under the action of a catalyst2(ii) a The main reaction mechanism of the two methods is:
(1)CmHn+mH2O＝mCO+1/2(n+2m)H2main reaction, endothermic reaction
(2)CO+H2O＝CO2+H2Side reactions, endothermic reactions
The non-catalytic reforming conversion reforming does not need a catalyst, pure oxygen is introduced into the mixed gas, and part of hydrocarbons in the mixed gas react with the pure oxygen to obtain CO and H2The main reaction mechanism is as follows: CH (CH)4+1/2O2→CO+2H2Hydrocarbons other than methane with methane and O2The reaction mechanism of (3) is similar.
Therefore, preferably, the reforming conversion process is a partial catalytic oxidation, wherein the partial catalytic oxidation is to introduce pure oxygen and steam into the mixed gas, and a part of hydrocarbons in the mixed gas react with the steam at the temperature of 850-1300 ℃ and in the presence of a catalyst to obtain CO and H2。
Preferably, the reforming conversion process is steam catalytic reforming conversion, the steam catalytic reforming conversion is to introduce steam into the mixed gas, under the conditions of indirect heat supply to make the temperature reach 850-2。
Preferably, the reforming conversion process is non-catalytic reforming conversion, the non-catalytic reforming conversion is that pure oxygen is introduced into the mixed gas, and part of hydrocarbons in the mixed gas react with the pure oxygen to obtain CO and H2。
After the reforming conversion process is adopted for treatment, H in the obtained synthesis gas2The volume ratio percentage of the CO and the CO is greatly improved, and the heat value of the synthetic gas is high.
Preferably, a gasification feeding system process is arranged between the drying process and the gasification reduction process, and the dried low-rank coal can be gasified and dispersed by adopting the process, so that the heating area of the low-rank coal in the gasification reduction process is increased.
Based on the technical scheme, the method for preparing upgraded coal, synthesis gas and coal tar from low-rank coal, which is disclosed by the invention, prepares the upgraded coal, the synthesis gas and the coal tar by developing and utilizing the low-rank coal in a grading and quality-dividing manner, has multiple product types, and is low in volatile content and high in quality in the obtained upgraded coal; the yield of the obtained coal tar is high; the obtained synthesis gas has high yield and high heat value, and fully and effectively utilizes effective resources in low-rank coal.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the embodiments will be briefly described below, it is obvious that the drawings in the following description are only some embodiments described in the present invention, and other drawings can be obtained by those skilled in the art according to the drawings.
FIG. 1 is a schematic flow diagram of a process for producing upgraded coal, syngas, and coal tar from low rank coal.
Detailed Description
The present invention is further illustrated by the following examples, which are not intended to limit the invention to these embodiments. It will be appreciated by those skilled in the art that the present invention encompasses all alternatives, modifications and equivalents as may be included within the scope of the claims.
In the present invention, unless otherwise specified, the processes in the following methods are all conventional in the art, unless otherwise specified.
As shown in FIG. 1, the invention provides a method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal, and the treatment method comprises the following steps: the low-rank coal is sequentially treated by a drying process and a gasification reduction process to obtain upgraded coal with temperature and an oil-gas mixture, the upgraded coal with temperature is treated by a cold slag humidifying process to obtain upgraded coal, the oil-gas mixture is subjected to a purification process to obtain mixed gas and coal tar, and the mixed gas contains CO and H2And hydrocarbons, wherein the gasification reduction process is a chemical reaction process for heating the dried low-rank coal under the oxygen-free or micro-oxygen condition, and the gasification reduction process is two-stage;
the mixed gas is treated by partial hydrocarbon reforming conversion process to obtain the mixed gas containing CO and H2The synthesis gas of (2).
The raw material low-rank coal can be pulverized coal or lump coal, and when the low-rank coal adopts the lump coal, the pulverized coal with smaller granularity can be obtained by crushing and screening the oversize lump coal. The pulverized coal is preferably used as a raw material, on one hand, the pulverized coal does not need to be crushed and screened, so that the process steps are saved, the heating area is large during drying, the drying efficiency is high, and on the other hand, the pulverized coal is low in price compared with lump coal. Pulverized coal having a particle size of less than 20mm is preferably used, and pulverized coal having a particle size of less than 6mm is still more preferably used.
The low-rank coal generally has 20-55% of volatile components, about 3-15% of tar, 30-60% of fixed carbon, 10-40% of water and the balance of other impurities such as dust. The low-rank coal has low coalification degree but contains abundant oil and gas resources, and the volatile components in the low-rank coal are very beneficial to extracting the synthesis gas, so that the low-rank coal with the volatile components between 30% and 55% is preferred.
If the low-rank coal contains a large amount of moisture, the heat consumption in the gasification reduction reaction process is large, so the technical scheme of the invention preferably treats the low-rank coal through a drying process. The drying medium of the drying process can be flue gas or water vapor, and the drying can be divided into direct drying and indirect drying. When flue gas is used as a drying medium, although the drying efficiency of the flue gas in direct contact with low-rank coal is the highest, the volume percentage of oxygen in the drying process environment is strictly controlled to be below an explosion limit when the flue gas is used for drying so as to prevent deflagration, and the efficiency of flue gas indirect drying is not ideal, so that steam drying is preferred for production safety and drying efficiency. The direct drying of the water vapor is easy to cause the water vapor to react with the low-rank coal to consume resources, so the drying mode of indirectly drying the low-rank coal by the water vapor is adopted to prevent the moisture in the water vapor from entering the low-rank coal. In addition, if the pressure of the steam is too high in the drying process, the temperature caused by the steam is too high, so that partial volatile components in the low-rank coal can escape out in the drying process, on one hand, the escape of the volatile components can bring potential safety hazards, and on the other hand, the gas yield of a subsequent gasification reduction process can be influenced, therefore, the drying steam pressure is not too high in the drying process, the drying effect can be guaranteed, and the volatile components in the low-rank coal can be prevented from being gasified. Therefore, preferably, the drying process adopts indirect drying by using water vapor, the pressure of the water vapor is 0.3-1.5Mpa, the temperature of the water vapor is 105-250 ℃, the water content in the low-rank coal can be reduced to the maximum extent under the process condition, even the water content in the low-rank coal discharged from a discharge port of the drying process can be reduced to be below 7 wt%, the temperature of an outlet material of the drying process is 50-150 ℃, and the water removed by the drying process forms waste gas along with dust such as coal dust and the like in the drying process in the form of the water vapor; still further preferably, when the pressure of the water vapor is 0.6-1.2Mpa and the temperature of the water vapor is 120-200 ℃, the water content of the dried low-rank coal is reduced to below 6 wt%, and the temperature of the outlet material of the drying process is 80-130 ℃.
The drying process can be one-stage or multi-stage, because if the water content of the low-rank coal after the first-stage drying process still does not meet the process requirement, multi-stage drying such as secondary drying, tertiary drying and the like can be adopted to continue further drying until the water content of the dried low-rank coal meets the process condition. In addition, the multistage drying process can be arranged in series or in parallel, the drying effect can be enhanced when the multistage drying process is connected in series, and the treatment capacity of the drying process can be increased when the multistage drying process is connected in parallel, so that the design that the multistage drying process is connected in series or in parallel or in series and in parallel can be adjusted according to the actual situation according to the requirement of the actual production process as long as the same technical effect can be achieved, and specifically, for example, when the feeding capacity of the drying process is calculated by low-rank coal of 20-30t/h, a one-stage steam drying process can be adopted; when the feeding amount of the drying process is calculated by a low level of 50-70t/h, a secondary steam drying process can be adopted, so that the method is more economical and reasonable.
The low-rank coal dried by the drying process is conveyed to the gasification reduction process for reaction, and a gasification feeding process can be added before the dried low-rank coal enters the gasification reduction process, so that the dried low-rank coal can rapidly enter the gasification reduction process, the surface area of the material is increased, and the gasification reduction reaction is accelerated.
Wherein, the gasification reduction process is a chemical reaction process for heating the dried low-rank coal under the condition of no oxygen or micro oxygen. The dried low-rank coal is conveyed to a gasification reduction process, under the heating of heating media such as flue gas and the like, additives and other substances are not needed to be added in the reaction process, the temperature is generally 350-800 ℃, and the pressure is less than or equal to 30Kpa, a complex chemical reaction process is carried out, so that a solid carbon and high-temperature oil-gas mixture is obtained, wherein the solid carbon is the upgraded coal with the temperature, and the volatile content in the upgraded coal with the temperature is 8-15 wt%. The high-temperature oil-gas mixture contains CO and H2、CO2Hydrocarbon, coal tar, dust, sulfur compounds, and the like.
Wherein, the oxygen-free or micro-oxygen environment adopted by the gasification reduction process is mainly divided into the following conditions: (1) air entrained in the gaps inside the raw material low-rank coal and the gaps between the materials, and O in the air2In the gasification ofThe coal reacts immediately in the high-temperature environment in the reduction process to generate CO2Or CO; (2) a small amount of mixed air, oxygen of the air and trace O are leaked from a feed inlet, a discharge outlet and the like of the gasification reduction process2Reacts with coal immediately to generate CO in high-temperature environment in gasification reduction process2Or CO; (3) under the explosion limit value, O accounting for 5 percent of the coal by mass can be slightly introduced into the gasification reduction process2Alternatively (air), this operation has the advantages of ① increased temperature and energy utilization in the gasification reduction process, ② increased char conversion, ③ prevention of coal coking, ④ small amount of O2The incomplete combustion with low-rank coal generates more CO, and more synthesis gas is brought to follow-up. Because the internal temperature of the gasification reduction process is higher, a small amount of O is introduced2Oxidation reactions (including combustion reactions) occur instantaneously, and the ignition point of many combustibles is below the reaction temperature of the gasification reduction reaction. Because the mixed explosion limit of CO and air is 12-74.2%; h2The explosion value is 4-75%. O is2The duty ratio is 21%. The upper explosion limit value of the converted pure oxygen is about 6 percent. By theoretical calculation, 100kg of coal will yield about 80Nm3CO and H of2. Therefore, introducing O accounting for 5 percent of the coal by mass2Is safe; further preferably, introducing O accounting for 3 percent of the mass of the coal2So as to ensure the safety and stability of the whole gasification reduction process reaction. However, when the temperature of the gasification reduction reaction meets the process requirements, oxygen may not be introduced, and the gasification reduction reaction of the dried low-rank coal is preferably performed in an oxygen-free environment, so that the reaction can be safely performed.
Wherein, the gasification reduction process can be one-stage or multi-stage. When a first-stage gasification reduction process is adopted, mainly aiming at obtaining most of high-temperature oil-gas mixture, the temperature directly influences the subsequent gas production, the yield of the upgraded coal with temperature and the temperature of the first-stage upgraded coal with temperature, the reaction temperature of the gasification reduction process is 350-800 ℃, the volatile content in the upgraded coal with temperature is 8-15 wt%, and further preferably, the reaction temperature of the gasification reduction process is 400-750 ℃; still more preferably 450-700 ℃. When the multistage gasification reduction process is adopted, the multistage gasification reduction process mainly has the main effects that solid matters (including gasified pulverized coal, solid impurities and the like) which cannot be gasified in the previous stage gasification reduction process and a certain amount of high-boiling-point oily matters such as similar asphalt and the like which cannot be gasified in a certain retention time are continuously gasified, the retention time is short and precipitation is not reached or the temperature does not reach the polycondensation reaction conditions of phenolic compounds, aromatic hydrocarbon compounds and the like, the reaction and gasification are continuously carried out, and the gas yield and the quality of upgraded coal are favorably improved.
Besides ensuring reasonable temperature of the gasification reduction process, certain retention time in the gasification reduction process is ensured, the retention time is too short, volatile components are not completely escaped for gasification, and the quality of upgraded coal with temperature is influenced more while the gas yield is influenced; the residence time is too long, and although the product is guaranteed, the yield cannot be kept up to, so that maintaining a reasonable residence time for the gasification reduction reaction is critical to the yield and quality of the product. Due to different varieties of raw material low-rank coal, the retention time of materials in the general gasification reduction process is 30min-4 h.
The two-stage gasification reduction process is optimized, the materials dried by the drying process enter the first-stage gasification reduction process and then enter the second-stage gasification reduction process, the dried low-rank coal enters the first-stage gasification reduction process to obtain first-stage gas and first-stage solid, the first-stage solid enters the second-stage gasification reduction process to be continuously gasified to obtain second-stage gas and second-stage solid, and the second-stage solid is upgraded coal with temperature; the feeding temperature of the first-stage gasification reduction process is 80-120 ℃, the gas outlet temperature is 180-550 ℃, the reaction temperature is 450-650 ℃, the discharging temperature is 350-600 ℃, and the volatile content in the first-stage object after the reaction is 8-15 wt%; the feeding temperature of the secondary gasification reduction process is 350-600 ℃, the discharging temperature is 450-750 ℃, the reaction temperature is 550-800 ℃, and the gas outlet temperature is 450-700 ℃. A two-stage gasification reduction process is adopted, which mainly aims to completely gasify most of volatile matters, so that a large amount of gas can be obtained, and the warmed upgraded coal with lower volatile matters can be obtained, wherein the volatile matter content in the warmed upgraded coal is 3-8 wt%.
The temperature of the upgraded coal with temperature obtained from the secondary gasification reduction process is higher, because the upgraded coal with temperature contains a small amount of volatile components, and the obtained upgraded coal with temperature is generally 45-65 wt% of the raw material low-rank coal, so that the yield of the obtained upgraded coal with temperature is high. The temperature of the upgraded coal with the temperature is generally 350-800 ℃, and the upgraded coal with the temperature does not contain water, and the upgraded coal with the temperature is exposed in the air, so that the upgraded coal with the temperature is easy to react with oxygen in the air, and a large amount of coal substances are consumed, therefore, the upgraded coal with the temperature is cooled and humidified by a slag cooling and humidifying process to prepare the upgraded coal which is normal temperature and contains a certain amount of moisture, the moisture content in the upgraded coal is about 10 wt%, and the upgraded coal is convenient to store, transport and sell.
The high-temperature oil-gas mixture obtained from the gasification reduction process enters a purification process for treatment. The purification process comprises a dust removal process, a cooling process, an oil-water separation process and a desulfurization process, wherein the high-temperature oil-gas mixture contains a large amount of dust, coal tar, water vapor, sulfur-containing compounds and the like; firstly, a dust removal process is utilized for removing dust, so that the temperature of an oil-gas mixture is prevented from being reduced in the dust removal process, and coal tar, water vapor and the like are condensed into liquid and adhered with a large amount of dust to cause the blockage of a subsequent process pipeline and the reduction of the dust removal effect; condensing the gas coal tar and water vapor in the oil-gas mixture into a liquid oil-water mixture by using a cooling process, and treating the oil-water mixture by using an oil-water separation process to obtain the coal tar product, wherein the coal tar is brown and has a relative density of about 0.85kg/m3The main components are cyclane, alkane, aromatic compound and the like, and the recovery rate of the coal tar is 80-95 percent, so that the yield of the obtained coal tar is high; and finally, removing sulfur-containing compounds from the residual gas after the cooling process through a desulfurization process, so as to prevent the sulfur-containing compounds from causing catalyst poisoning in the subsequent process.
In order to further optimize the process, an electric tar capturing process can be additionally arranged after the desulfurization process for capturing a small amount of tar so as to further reduce the amount of tar in the gas; if the volume fraction of the unsaturated hydrocarbon in the oil-gas mixture is too high, a hydrogenation process can be added after the desulfurization process to convert the unsaturated hydrocarbon into saturated hydrocarbon, so that the problems of carbon deposition and the like caused by the decarbonization of the unsaturated hydrocarbon are prevented; and a denitration process or a dechlorination process can be added after the desulfurization process to realize further purification.
The invention adopts two-stage gasification reduction process, and each stage of gasification reduction process is respectively connected with respective dust removal process, cooling process, oil-water separation process, desulfurization process and the like; the dust amount in the high-temperature oil gas generated after gasification and reduction is large, so that in order to further optimize the process, each stage of gasification and reduction process is connected with the respective dust removal process, and the dust removal process of each stage is connected with the same set of cooling process, oil-water separation process and desulfurization process, so that the process links are saved.
It is further preferred that the mixed gas is compressed before entering the reforming process, so as to better perform the reforming reaction.
The mixed gas obtained from the purification process enters a reforming conversion process for treatment to obtain the product containing CO and H2The synthesis gas of (2). Wherein the mixed gas comprises CO and H2、CO2And comprises CH4And the like.
The mixed gas is reformed and converted into CO and H through partial hydrocarbon to obtain the mixed gas with various components without separation2Because the reforming conversion is only intended to convert hydrocarbons to CO and H2The mixed gas already contains a part of CO and H2Therefore, the hydrocarbon does not need to be separated from the mixed gas and then reformed and converted, and the operation saves the process steps and has high economic benefit.
Reforming conversion mainly includes partial catalytic oxidation, steam catalytic reforming conversion, and non-catalytic reforming conversion. The catalyst is needed for partial catalytic oxidation and steam catalytic reforming conversion, the catalyst for reforming conversion process is mostly a load type catalyst, and the active components are mainly non-metals such as Ni, Co, Fe, Cu and the like and noble metals such as Rh, Ru, Pt and the like. Reforming conversion is generally required to supplyThe heat can be directly supplied or indirectly supplied. CO and H in syngas2The source of the (C) is two parts, one part is CO and H obtained by catalytic conversion of partial hydrocarbons in the mixed gas2The other part is original H in the mixed gas2And CO.
The partial catalytic oxidation adopts oxygen and partial hydrocarbon to burn and directly supply heat, so that the reaction temperature reaches 850-1300 ℃, and partial hydrocarbon in the mixed gas reacts with steam to generate CO and H under the action of the catalyst2(ii) a When the steam catalytic reforming conversion is carried out, external heat supply is adopted, the temperature is up to 850-1200 ℃, and partial hydrocarbons in the mixed gas react with steam to generate CO and H under the action of a catalyst2(ii) a The main reaction mechanism of the two methods is:
(1)CmHn+mH2O＝mCO+1/2(n+2m)H2main reaction, endothermic reaction
(2)CO+H2O＝CO2+H2Side reactions, endothermic reactions
With CH4For example, the main reaction equation is CH4+H2O→CO+3H2Generation of H2The molar ratio of CO to CO is 3:1, and the ratio is large, so that the method is very favorable for preparing the synthesis gas.
The non-catalytic reforming conversion reforming does not need a catalyst, pure oxygen is introduced into the mixed gas, and part of hydrocarbons in the mixed gas react with the pure oxygen to obtain CO and H2The main reaction mechanism is as follows: CH (CH)4+1/2O2→CO+2H2Generation of H2And CO in a molar ratio of 2:1, which is favorable for preparing the synthesis gas. Hydrocarbons other than methane with methane and O2The reaction mechanism of (3) is similar.
Table 1: the range value of the volume percentage of each component in the mixed gas before reforming conversion is as follows:
| components | H2 | Comprising CH4Of (2) | CO | CO2 | Others |
| Content (wt.) | 15-45％ | 10-52％ | 5-25％ | 5-25％ | 0.1-10％ |
The other component is N2And steam, etc., the volume percentages of the components in the mixed gas before reforming conversion are integrated to 100%.
Table 2: the range value of the volume percentage of each component in the mixed gas after reforming conversion is as follows:
| components | H2 | Comprising CH4Of (2) | CO | CO2 | Others |
| Content (wt.) | 30-70％ | 1-5％ | 10-30％ | 3-35％ | 0.1-10％ |
The other component is N2And steam, etc., the volume percentage of each component in the mixed gas after reforming conversion is integrated to be 100%.
As no external substances are basically added in the process of the gasification reduction process, the weight of the mixed gas obtained after the low-rank coal is treated by the drying process, the gasification reduction process and the purification process is 15-50% of the volatile components of the low-rank coal according to the mass conservation law, so that the method can prove that the gas in the low-rank coal is basically completely gasified and the yield of the obtained mixed gas is high. As can be seen from tables 1 and 2, the volume percentage of the hydrocarbons in the mixed gas is reduced from 10-52% to 1-5% after the mixed gas is treated by the reforming conversion process, the mixed gas after reforming conversion is the synthesis gas, and CO and H in the synthesis gas2The sum of the volume percentages of the components is 60-80%, and the heat value in the synthesis gas is greatly improved.
In conclusion, the invention provides a method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal, wherein the method for treating the low-rank coal is used for preparing the upgraded coal, the synthesis gas and the coal tar by developing and utilizing the low-rank coal in a grading and quality-dividing manner, the product types are various, and the obtained upgraded coal has less volatile components and high quality; the yield of the obtained coal tar is high; the obtained synthesis gas has high yield and high heat value, and fully and effectively utilizes effective resources in low-rank coal.
The above-mentioned embodiments are only used for illustrating the technical solutions of the present invention, and not for limiting the same; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. A method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal comprises the following steps: the method comprises the steps that low-rank coal is sequentially treated through a drying process and a gasification reduction process to obtain upgraded coal with temperature and an oil-gas mixture, the upgraded coal with temperature is treated through a cold slag humidifying process to obtain upgraded coal, the oil-gas mixture is subjected to a purification process to obtain mixed gas and coal tar, and the mixed gas contains CO and H2And hydrocarbons characterized by: the gasification reduction process is a chemical reaction process for heating the dried low-rank coal under the condition of no oxygen or micro oxygen, and the gasification reduction process is two-stage;
the mixed gas is treated by partial hydrocarbon reforming conversion process to obtain the mixed gas containing CO and H2The synthesis gas of (2).
2. The method for producing upgraded coal, syngas and coal tar from low-rank coal according to claim 1, wherein the method comprises the following steps: the drying process adopts water vapor for indirect drying, the pressure of the water vapor is 0.3-1.5Mpa, the temperature of the water vapor is 105-250 ℃, the water content of the outlet material of the drying process is not more than 7 wt%, and the temperature of the outlet material of the drying process is 50-150 ℃.
3. The method for producing upgraded coal, syngas and coal tar from low-rank coal according to claim 2, wherein the method comprises the following steps: the drying process adopts water vapor for indirect drying, the pressure of the water vapor is 0.6-1.2Mpa, the temperature of the water vapor is 120-200 ℃, the water content of the outlet material of the drying process is not more than 6 wt%, and the temperature of the outlet material of the drying process is 80-130 ℃.
4. The method for producing upgraded coal, syngas and coal tar from low-rank coal according to claim 1, wherein the method comprises the following steps: the feeding temperature of the primary gasification reduction process is 80-120 ℃, the reaction temperature of the primary gasification reduction process is 450-650 ℃, the gas outlet temperature of the primary gasification reduction process is 180-550 ℃, and the discharging temperature of the primary gasification reduction process is 350-600 ℃; the feeding temperature of the secondary gasification reduction process is 350-600 ℃, the reaction temperature of the secondary gasification reduction process is 550-800 ℃, the discharging temperature of the secondary gasification reduction process is 450-750 ℃, and the gas outlet temperature of the secondary gasification reduction process is 450-700 ℃.
5. The method for producing upgraded coal, syngas and coal tar from low-rank coal according to claim 1, wherein the method comprises the following steps: the purification process comprises a dust removal process, a cooling process, an oil-water separation process and a desulfurization process, wherein the oil-gas mixture is sequentially treated by the dust removal process, the cooling process and the desulfurization process to obtain a mixed gas and an oil-water mixture, and the mixed gas contains CO and H2And hydrocarbons, wherein the oil-water mixture is treated by an oil-water separation process to obtain coal tar.
6. The method for producing upgraded coal, syngas and coal tar from low-rank coal according to claim 1, wherein the method comprises the following steps: the mixed gas is reformed and converted into CO and H through partial hydrocarbon to directly reform and convert the partial hydrocarbon into the mixed gas without separating each component of the gas2The reforming conversion process of (1).
7. The method for producing upgraded coal, syngas and coal tar from low-rank coal according to claim 6, wherein the method comprises the following steps: the reforming conversion process is partial catalytic oxidation, wherein the partial catalytic oxidation is to introduce pure oxygen and steam into mixed gas, and part of hydrocarbons in the mixed gas react with the steam at the temperature of 850-To obtain CO and H2。
8. The method for producing upgraded coal, syngas and coal tar from low-rank coal according to claim 6, wherein the method comprises the following steps: the reforming conversion process is steam catalytic reforming conversion, the steam catalytic reforming conversion is to introduce steam into mixed gas, under the conditions of indirect heat supply to make the temperature reach 850-1200 ℃ and the existence of catalyst, partial hydrocarbons in the mixed gas react with the steam to obtain CO and H2。
9. The method for preparing the synthesis gas by using the low-rank coal as claimed in claim 6, wherein the method comprises the following steps: the reforming conversion process is non-catalytic reforming conversion, the non-catalytic reforming conversion is to introduce pure oxygen into mixed gas, and partial hydrocarbons in the mixed gas react with the pure oxygen to obtain CO and H2。
10. The method for preparing the synthesis gas by using the low-rank coal as claimed in claim 1, wherein the method comprises the following steps: and a gasification feeding system process is arranged between the drying process and the gasification reduction process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811459025.2A CN111253977A (en) | 2018-11-30 | 2018-11-30 | Method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811459025.2A CN111253977A (en) | 2018-11-30 | 2018-11-30 | Method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111253977A true CN111253977A (en) | 2020-06-09 |
Family
ID=70923584
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811459025.2A Pending CN111253977A (en) | 2018-11-30 | 2018-11-30 | Method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111253977A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4317703A (en) * | 1980-12-03 | 1982-03-02 | American Can Company | Pyrolysis process utilizing pyrolytic oil recycle |
| JP2005319373A (en) * | 2004-05-07 | 2005-11-17 | Tokyo Electric Power Co Inc:The | Method and apparatus for converting sludge into fuel |
| CN101538473A (en) * | 2009-04-01 | 2009-09-23 | 上海胜帮煤化工技术有限公司 | Incoherence or weak caking coal deep processing method |
| CN103205276A (en) * | 2013-04-08 | 2013-07-17 | 石家庄新华能源环保科技股份有限公司 | System for producing clean energy |
| CN105950196A (en) * | 2016-05-19 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | System using coal pyrolysis and splitting to produce synthesized gas |
-
2018
- 2018-11-30 CN CN201811459025.2A patent/CN111253977A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4317703A (en) * | 1980-12-03 | 1982-03-02 | American Can Company | Pyrolysis process utilizing pyrolytic oil recycle |
| JP2005319373A (en) * | 2004-05-07 | 2005-11-17 | Tokyo Electric Power Co Inc:The | Method and apparatus for converting sludge into fuel |
| CN101538473A (en) * | 2009-04-01 | 2009-09-23 | 上海胜帮煤化工技术有限公司 | Incoherence or weak caking coal deep processing method |
| CN103205276A (en) * | 2013-04-08 | 2013-07-17 | 石家庄新华能源环保科技股份有限公司 | System for producing clean energy |
| CN105950196A (en) * | 2016-05-19 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | System using coal pyrolysis and splitting to produce synthesized gas |
Non-Patent Citations (3)
| Title |
|---|
| 周安宁等主编: "《洁净煤技术》", 28 February 2018, 中国矿业大学出版社 * |
| 孟献梁等主编: "《煤炭加工利用概论》", 31 January 2018, 中国矿业大学出版社 * |
| 湖北辞书出版社, 湖北辞书出版社 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101787291B (en) | High-efficiency and quick lignite pyrolysis method | |
| CN101657525A (en) | System and method for producing substitute natural gas from coal | |
| CN105154121A (en) | Low-rank coal gradation usage poly-generation system and method | |
| JP2013522422A (en) | Method and system for producing synthesis gas from biomass by carbonization | |
| CN109652139A (en) | A kind of method and system preparing synthesis gas using volatile matter in low-order coal and waste water | |
| CN107474859B (en) | Coal pyrolysis gasification process coupling device and method thereof | |
| CN205133505U (en) | Low order coal grading utilizes many cogeneration system | |
| CN110055106B (en) | Method for preparing methanol and oil by poly-generation through low-rank coal quality-based utilization | |
| CN109762603A (en) | A method of ammonia is synthesized using low-order coal multipath | |
| CN110862841B (en) | Method for preparing natural gas from coal water slurry | |
| CN111253975A (en) | Method for grading and utilizing low-rank coal | |
| CN111253977A (en) | Method for preparing upgraded coal, synthesis gas and coal tar by using low-rank coal | |
| CN210885959U (en) | System for preparing synthesis gas by low-rank coal gasification reduction | |
| CN111253972A (en) | Low-rank coal treatment method | |
| CN110002933B (en) | Method for preparing methanol and low-carbon olefin by poly-generation through low-rank coal quality-based utilization | |
| CN111253976A (en) | Method for treating low-rank coal | |
| CN101838558B (en) | Mixed fuel coal water slurry entrained flow bed gasification system | |
| CN109762612A (en) | A method of using waste water water-coal-slurry and passing through water-coal-slurry methanol | |
| CN201737900U (en) | High-efficiency quick coal pyrolyzing device | |
| CN110093174A (en) | A kind of method of low-order coal hydrogen manufacturing | |
| CN115125044B (en) | Method for preparing oil product and co-producing electricity by using low-rank coal and natural gas | |
| CN211311390U (en) | System for preparing synthesis gas by reforming and converting low-rank coal | |
| CN111253971A (en) | Method and system for utilizing water resources in low-rank coal | |
| CN110564437A (en) | system and method for improving quality of coal in front of pulverized coal furnace | |
| CN111321010A (en) | Method and system for preparing synthesis gas by utilizing low-rank coal in multiple ways |
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 | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200609 |