CN107189803B - System and method for co-production of low-carbon alcohol and fuel oil product by coal-based LNG (liquefied Natural gas) - Google Patents
System and method for co-production of low-carbon alcohol and fuel oil product by coal-based LNG (liquefied Natural gas) Download PDFInfo
- Publication number
- CN107189803B CN107189803B CN201710388523.1A CN201710388523A CN107189803B CN 107189803 B CN107189803 B CN 107189803B CN 201710388523 A CN201710388523 A CN 201710388523A CN 107189803 B CN107189803 B CN 107189803B
- Authority
- CN
- China
- Prior art keywords
- subsystem
- gas
- coal
- low
- rich
- 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.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/006—Combinations of processes provided in groups C10G1/02 - C10G1/08
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/008—Controlling or regulating of liquefaction processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
-
- 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
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural 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
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
-
- 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
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
-
- 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
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
-
- 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
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- 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
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A system and a method for coproducing low-carbon alcohol and fuel oil products by using coal LNG are characterized in that low-rank coal resources are converted into high-quality medium-low temperature coal tar and methane-rich synthetic gas in a one-step method, and high-quality medium-low temperature coal tar and CH are obtained on the basis 4 Purifying the synthetic gas, and converting the high-quality medium-low temperature coal tar into clean liquid fuel oil product, CH, through deep conversion processing 4 The LNG can be produced after purification and cryogenic pressurization, and the purified synthesis gas enters a low-carbon alcohol synthesis system to produce low-carbon mixed alcohol. Therefore, the quality-grading and grading conversion of low-rank coal resources can be fundamentally realized based on the invention, and the high-efficiency clean conversion of the coal resources and the maximization of economic benefit can be realized through the constructed multi-industry coupling integration mode.
Description
Technical Field
The invention relates to the field of low-rank coal resource quality-based and graded utilization, coal-based LNG co-production coal-based chemicals and liquid fuels, in particular to a system and a method for coal-based LNG co-production low-carbon alcohol and fuel oil products.
Background
By 2050, the global population will grow to 90 billion, with 75% living in cities, at which time the demand for oil and gas will double. Energy transformation is particularly necessary to meet energy requirements and further reduce carbon dioxide emission. Therefore, the development of renewable energy sources such as wind energy, solar energy and the like is also met with new opportunities, however, the renewable energy sources have the characteristics of discontinuity and discontinuity, are limited by geographical conditions, have higher cost, and are limited by bottlenecks in large-scale development. At present, the global energy transformation is just right, natural gas plays an important role in the transformation, and China will become the leading part of the international natural gas market in the future. Natural gas is the cleanest energy among fossil energy, and compared with renewable energy, the natural gas has the advantages of stability, reliability and cost, and plays an important role in the transformation process of an energy system. LNG can well connect natural gas demand and resource ground, and the global LNG market year acceleration rate will reach 5% in the future, surpasses the acceleration rate of global energy total demand and natural gas demand. Asia, especially china, is the most important LNG market worldwide. Driven by factors such as environmental requirements, consumption demands, energy structure improvement and the like, the Chinese consumption market has great growth potential. Currently, the primary energy demand in china is about 6% of natural gas, which is much lower than the average level of 20% worldwide. In the transportation field, about 20 million heavy trucks and buses driven by liquefied natural gas are currently available in China, the number of the heavy trucks and buses is more than 130 of that of European liquefied natural gas trucks, and about 2000 filling stations and 100 small natural gas liquefaction plants are available for supplying gas to the trucks.
According to the latest statistical data of the national reform committee, the annual natural gas yield of China in 2016 is about 1371 billions of cubic meters, and the gas yield is increased by 1.5 percent on year-on-year basis; the natural gas inlet amount is 720 billion cubic meters, and the increase is 17.4 percent; the natural gas consumption is 2090 billion cubic meters, the increase is 6.6 percent, and the external dependence of the natural gas is as high as 34.44 percent. In addition, in 2016, the total energy consumption of China is about 43.6 hundred million tons of standard coal: 38.9 million tons of raw coal (about 27.0 million tons of standard coal), 5.7 million tons of oil (about 8.1 million tons of standard coal), 2090 million cubic meters of natural gas (about 2.7 million tons of standard coal), and a total of about 11.6 million tons of standard coal for electric power, new energy, and the like. Wherein the coal consumption accounts for 61.9 percent, and the natural gas accounts for about 6.3 percent. In addition, in the energy resource reserves which are already explored at the present stage of China, the coal proportion is up to more than 94%, and the oil-gas resource proportion is only about 6%. Due to the consideration of the energy resource storage endowment and the energy safety strategy in China, coal is regarded as a main performance source substance in China, and the dominant position of the coal cannot be changed. At the present stage, the largest problems of the utilization of the coal resources in China are high direct combustion ratio and high pollutant emission intensity, so that the quality-divided and graded conversion of the coal resources is implemented, the production of coal-based clean fuels and chemicals is pushed forward, the production of chemical products of partial petroleum routes is replaced, and irreplaceable significance is provided for reducing the external dependence of the petroleum resources in China and the green consumption of the coal resources. The C1 chemical industry for producing liquid fuel and organic chemical products based on coal and natural gas has wide development prospect, and the preparation of low-carbon mixed alcohol from synthesis gas is a subject with important research significance and wide application prospect in the C1 chemical field. For example, the low-carbon alcohol prepared from coal and natural gas through synthesis gas has the excellent performances of high octane number, explosion resistance, shock resistance and the like, and is very suitable for being used as a gasoline additive, and meanwhile, the low-carbon alcohol is an important chemical raw material and an ideal high-octane number pollution-free vehicle fuel.
Patent CN101805242A discloses a method for continuously producing low carbon alcohol from synthesis gas, and discloses a process for producing low carbon alcohol by synthesis gas and producing corresponding alcohol by hydration of olefin. Patent CN 103553861A provides a system and a process for synthesizing methanol and co-producing methane by using synthesis gas, and realizes the production of methanol from coal and natural gas from coal. The methanol synthesis reactor and the methanation reactor are connected in series in one stage or multiple stages, the sequence of the two reactors can be adjusted, and the reasonable allocation of the methanol synthesis and methanation reactions of synthesis gas composed of different components can be realized. Patent CN101735008A discloses a technology for co-producing low carbon alcohol and natural gas from coal, which discloses a technology for combining a low carbon alcohol synthesis process and a methanation process, including several parts of gas purification, alcohol synthesis and collection, tail gas separation and methanation, etc., wherein one part of the tail gas from the synthesis of low carbon alcohol is recycled to the low carbon alcohol synthesizer, and the other part is used for synthesizing methane. The patent CN 105061141A discloses a process for preparing low-carbon mixed alcohol and co-producing urea and natural gas from synthesis gas, and discloses a technology for preparing low-carbon mixed alcohol, urea and natural gas from low-carbon coal by synthesis gas 2 With N from space division 2 The synthetic ammonia, the synthetic ammonia and CO are obtained in a synthetic ammonia unit 2 And entering a urea synthesis unit to obtain the synthetic urea. The patent CN101805242A discloses a method for continuously producing low-carbon alcohol by synthesis gasThe invention discloses a process for producing low carbon alcohol by synthesis gas and hydrating olefin to generate corresponding alcohol. CN101735009A discloses a sulfur-tolerant catalysis process for preparing low-carbon alcohol and co-producing natural gas from synthesis gas, which discloses a process for combining a sulfur-tolerant low-carbon alcohol synthesis process with a natural gas production process through sulfur-tolerant methanation, wherein the synthesis gas can be subjected to a low-carbon alcohol synthesis reaction without fine desulfurization, one part of tail gas is circulated back to a low-carbon alcohol synthesis reactor, and the other part of tail gas enters a methanation device to synthesize methane, so that the sulfur tolerance and poly-generation of the whole process are realized, and the economy of the device is improved to a certain extent. However, both the two technologies have the defects of low yield of the low-carbon alcohol, no separation of the low-carbon alcohol, high energy consumption and low yield of the target product. Although the invention patents mentioned above relate to the coupling process route of coal gasification and low carbon alcohol preparation from synthesis gas and natural gas phase preparation from synthesis gas, the step utilization of low-rank coal resources is not realized fundamentally, and the subsequent processes are grafted with the technologies of low carbon alcohol synthesis, ammonia synthesis, CNG process and the like. The biggest defect of the coal gasification process is that precious aromatic hydrocarbon resources contained in coal are not fully utilized, and the molecules of the coal gasification process are broken into the most basic CO and H 2 And then the subsequent synthesis gas chemical industry is carried out. The coal pyrolysis technology can reserve aromatic hydrocarbon resources in coal in a high-quality coal tar form to the maximum extent, and further realize the coupling integration of coal-based liquid fuel, gas fuel (natural gas) and a methanol/low-carbon alcohol polyhydric industry chain prepared from synthetic gas.
Disclosure of Invention
The invention aims to provide a system and a method for gradient utilization and efficient clean conversion of coal resources, namely, a system and a method for producing high-concentration methane-rich synthetic gas coal-based LNG and co-producing low-carbon alcohol and fuel oil products while producing high-quality medium and low-temperature coal tar through pressurized and rapid pyrolysis of pulverized coal.
To achieve the above object, the system of the present invention comprises: the system comprises a system for synchronously preparing the methane-rich synthesis gas and the light coal tar, a coal tar deep conversion system communicated with a coal tar outlet of the system for synchronously preparing the methane-rich synthesis gas and the light coal tar, a methane enrichment separation and cryogenic liquefaction system communicated with a methane-rich synthesis gas outlet of the system for synchronously preparing the methane-rich synthesis gas and the light coal tar, and a low carbon alcohol synthesis system;
the system for synchronously preparing the methane-rich synthesis gas and the light coal tar comprises a continuous pressurization steady-state feeding subsystem and a pulverized coal rapid pressurization thermal cracking reaction subsystem communicated with the continuous pressurization steady-state feeding subsystem, wherein a crude synthesis gas outlet of the pulverized coal rapid pressurization thermal cracking reaction subsystem is connected with a particle sieve molecular system, an outlet at the upper end of the particle sieve molecular system is connected with an oil-gas shunting subsystem, and an outlet at the lower end of the particle sieve molecular system is connected with the pulverized coal rapid pressurization thermal cracking reaction subsystem through a circulating particle control shunting subsystem;
the coal tar deep conversion system comprises a coal tar pretreatment subsystem, a raw oil fraction cutting subsystem, a distillate oil hydrogenation upgrading subsystem, a product separation and recovery subsystem and an oil product storage subsystem which are sequentially connected, wherein the coal tar pretreatment subsystem is communicated with a light coal tar outlet of the oil gas diversion subsystem;
the methane enrichment separation and cryogenic liquefaction system comprises a washing and purification subsystem, a molecular sieve adsorption subsystem, a light component purification and separation subsystem, a methane separation and purification subsystem, a cryogenic liquefaction subsystem and an LNG storage subsystem which are sequentially connected, wherein the washing and purification subsystem is communicated with a methane-rich synthetic gas outlet of the oil-gas diversion subsystem;
the low-carbon alcohol synthesis system comprises a raw material gas component regulation and control subsystem, a raw material gas purification subsystem, a low-carbon alcohol synthesis reaction subsystem, a low-carbon mixed alcohol separation subsystem, a product refining subsystem and a low-carbon alcohol storage subsystem which are sequentially connected, wherein the raw material gas component regulation and control subsystem is connected with an LNG (liquefied natural gas) storage subsystem outlet of the methane enrichment separation and cryogenic liquefaction system.
The continuous pressurization steady-state feeding subsystem comprises a raw material storage bin, a controllable feeding pulverizer, an integrated circulating gas dryer, a feeding buffer and a mechanical pneumatic coupling type pulverized coal feeding device which are sequentially connected, wherein the mechanical pneumatic coupling type pulverized coal feeding device is communicated with the coal rapid pressurization pyrolysis reaction subsystem.
The coal rapid pressurization and pyrolysis reaction subsystem 6 comprises a pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid pyrolysis reaction area, a mixed fluid temperature control area, a vortex flow field transmission area, a mixed fluid rectification area and a reaction area for preparing hydrogen-rich gas by secondary pyrolysis of circulating particles which are sequentially connected from top to bottom and can realize internal material and energy coupling, the vortex flow field transmission area is connected with a mechanical and pneumatic coupling type pulverized coal feeding device of the coal rapid pressurization and pyrolysis reaction subsystem, a methane-rich synthetic gas outlet of the pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid pyrolysis reaction area is connected with a particle sieve molecular system, and an outlet at the lower end of the particle sieve molecular system returns to the reaction area for preparing hydrogen-rich gas by secondary pyrolysis of the circulating particles through a circulating particle control shunting subsystem.
The particle screening subsystem is used for grading, segmenting and classifying the inert particles with the particle size of 50-600 mu m and the carbon-rich particles with the fixed carbon content of 60-80 wt% and the particle size of less than 50 mu m for recycling.
The circulating particle control and distribution subsystem forms a circulating flux of 1000-5000 kg/m based on a local jet configuration in the reactor through the coupling of an internal multi-channel particle circulating device and an external grading and sectional material returning system 2 S high rate particle cycle with 10-20MJ/m 2 S heat flux of 1 to 10ms, 10 3 ～10 5 And instantaneously heating the pulverized coal to the pyrolysis temperature of 500-700 ℃ at the temperature rise rate of K/s.
The composition of the methane-rich synthesis gas output by the oil-gas flow splitting subsystem is CO 30-41 vol%, and H 2 6～30vol％CH 4 8～30vol％，C m H n 0.1～0.2vol％CO 2 18～27vol％，N 2 2～5vol％。
The circulating particle control flow-dividing subsystem adopts water vapor and CO 2 One or more than two of synthetic gas, air, oxygen-enriched gas or pure oxygen are prepared into activating gas according to any proportion to activate the captured inert particles.
The operation pressure of the pulverized coal rapid pressurization thermal cracking reaction subsystem is 3.0-7.0 MPa, the reaction temperature range of a reaction zone for preparing hydrogen-rich gas by secondary cracking of circulating particles is 950-1200 ℃, and the reaction temperature range of a pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid thermal cracking reaction zone is 500-700 ℃.
The feed gas component regulates and controls the hydrogen-carbon ratio H of the low-carbon alcohol synthesis feed gas output by the subsystem 2 /CO＝2.10～4.8；
The final output product of the low-carbon alcohol synthesis system comprises the following components: 30-75 wt% of methanol, 8-13 wt% of ethanol, 2-10 wt% of propanol, 5-15 wt% of butanol/isobutanol, and C + 5 2-5 wt% of alcohol.
The method for producing LNG (liquefied natural gas) and coproducing low-carbon alcohol and fuel oil from coal comprises the following steps:
firstly, raw material coal in a raw material storage bin in a system for synchronously preparing methane-rich synthesis gas and light coal tar is crushed into pulverized coal particles with the particle size of 10-1000 mu m by a controllable feeding crusher, then the pulverized coal particles are dried by an integrated circulating gas dryer until the water content is lower than 2.0 wt% and enter a feeding buffer, then the pulverized coal particles are conveyed to a vortex flow field transfer area of a pulverized coal rapid pressurization and pyrolysis reaction subsystem by a mechanical-pneumatic coupling type pulverized coal feeding device, hydrogen-rich high-temperature gas-solid mixed heat carrier obtained from a reaction area for preparing hydrogen-rich gas by secondary pyrolysis of the circulating particles and inert particles returned by a built-in multi-channel material returning system are uniformly mixed in a mixed fluid rectifying area, the temperature is reduced to about 600 ℃, the pulverized coal continuously ascends into the vortex flow field transfer area and is mixed with fresh pulverized coal, then ascends at a high speed into a mixed fluid temperature control area to complete rapid heat transfer, the pulverized coal is heated to the preset pyrolysis temperature of 550-600 ℃, and then continuously ascends into constant-temperature pulverized coal-pressurization-catalysis Pyrolyzing in a hydrogenation rapid thermal cracking reaction zone;
secondly, the coal dust particles are converted into tar steam, methane, CO and H by a one-step method in a system for synchronously preparing the methane-rich synthesis gas and the light coal tar 2 、CO 2 And a small amount of raw synthesis gas composed of other components, particles with different attributes in the raw synthesis gas are collected by a particle sieve molecular system and then returned to different reaction areas of the pulverized coal rapid pressurization thermal cracking reaction subsystem in a grading, segmentation and classification mode through a circulating particle control shunting subsystem, wherein carbon-rich particles are circularly returned to a reaction area for preparing hydrogen-rich gas through secondary cracking of circulating particles, the reaction area is used for preparing hydrogen-rich synthesis gas and is used as a hydrogen source for the hydro-pyrolysis of the pulverized coal constant-temperature-pressurization-catalytic hydrogenation rapid thermal cracking reaction area, and the products output by the system for synchronously preparing the methane-rich synthesis gas and the light coal tar are respectively liquid high-quality medium-low temperature coal tar and gaseous methane-rich synthesis gas;
then, the product of the pulverized coal constant-temperature, pressurizing and catalytic hydrogenation rapid thermal cracking reaction zone of the pulverized coal rapid pressurizing thermal cracking reaction subsystem is sent to the oil-gas shunting subsystem after passing through a particle sieve molecular system, the low-temperature coal tar shunted by the oil-gas shunting subsystem enters a coal tar pretreatment subsystem of a coal tar deep conversion system at the downstream for dust removal, dehydration, desalination and purification, and then enters a raw oil fraction cutting subsystem to cut the purified coal tar into light distillate, medium distillate and heavy distillate; the distillate oil with different distillation ranges enters a subsequent distillate oil hydrogenation upgrading subsystem to be finally converted into clean fuel oil products with high added values and fine chemical products, and the clean fuel oil products and the fine chemical products are sent to an oil product storage subsystem;
the methane-rich synthetic gas after the recovery and dust removal purification treatment of the medium and low temperature coal tar is used for removing CO in the synthetic gas from the oil gas diversion subsystem to the washing and purification subsystem of the methane enrichment separation and cryogenic liquefaction system 2 、H 2 S, COS and other acid gas impurities enter a molecular sieve adsorption subsystem for deep purification and removal of CH in the synthesis gas 3 OH、H 2 O、CO 2 The trace impurities are equal to obtain the main component H 2 、CO、CH 4 The methane-rich purified synthesis gas enters a subsequent light component purification and separation subsystem, a methane separation and purification subsystem and a cryogenic liquefaction subsystem, and an LNG product with the final methane concentration of more than 97 vol% is sent to an LNG storage subsystem;
finally, methane enrichment separation and cryogenic liquefaction systemDe-CH output by LNG storage subsystem 4 The synthesis gas enters a raw material gas component regulation subsystem of a downstream low-carbon alcohol synthesis system to regulate the hydrogen-carbon ratio in the synthesis gas to 2.10-4.8, and the synthesis gas after the hydrogen-carbon ratio regulation enters a raw material gas purification subsystem to remove CO 2 、H 2 And O and other impurities, and the output qualified raw material gas enters the low-carbon alcohol synthesis reaction subsystem, and the low-carbon mixed alcohol produced by the low-carbon alcohol synthesis reaction subsystem sequentially passes through the low-carbon mixed alcohol separation subsystem and the product refining subsystem and then is sent to the low-carbon alcohol storage subsystem.
Compared with the process technical route disclosed by the invention patent, the invention firstly converts low-rank coal resources into high-quality medium-low temperature coal tar and methane-rich synthesis gas by one step, and obtains the high-quality medium-low temperature coal tar and CH on the basis 4 Purifying the synthetic gas, and converting the high-quality medium-low temperature coal tar into clean liquid fuel oil product, CH, through deep conversion processing 4 The LNG can be produced after purification and cryogenic pressurization, and the purified synthesis gas enters a low-carbon alcohol synthesis system to produce low-carbon mixed alcohol. Therefore, the quality-grading and grading conversion of low-rank coal resources can be fundamentally realized based on the invention, and the high-efficiency clean conversion and the maximization of economic benefit of the coal resources can be realized through the constructed multi-industry coupling integration mode.
Compared with the existing gasification process matched with coal-based natural gas, the device and the method disclosed by the invention have the following advantages:
1) the method is characterized in that pulverized coal is used as a raw material, and methane-rich synthetic gas and high-quality medium-low temperature coal tar are synchronously produced through rapid hydropyrolysis of the pulverized coal, wherein the concentration of methane in the produced synthetic gas is up to 8-30 vol% and is higher than that of methane in crude synthetic gas produced by the conventional pulverized coal pressure gasification technology, so that the scale and investment of a subsequent methanation device are greatly reduced;
2) the yield of the light coal tar in the process technology system disclosed by the invention is up to 15-20 wt%, and the light coal tar can be highly coupled and integrated with a downstream coal tar deep processing industrial chain, so that the overall economic competitiveness of the process system is greatly improved;
3) the process technology system and the method disclosed by the invention can realize the coupling of multiple industrial chains of low-carbon mixed alcohol prepared from LNG prepared from coal, low-carbon mixed alcohol prepared from synthesis gas and clean liquid fuel prepared from medium-low temperature coal tar through deep processing, and greatly improve the overall economic competitiveness of the process system.
Drawings
FIG. 1 is a schematic diagram of the apparatus and process of the present invention.
In the figure: 1. a system for synchronously preparing the methane-rich synthesis gas and the light coal tar; 2. a coal tar deep conversion system; 3. a methane enrichment separation and cryogenic liquefaction system; 4. a low carbon alcohol synthesis system; 5. a continuous pressurized steady state feed subsystem; 6. a pulverized coal rapid pressurization thermal cracking reaction subsystem; 7. a particle screening subsystem; 8. a circulating particle control shunt subsystem; 9. storing the raw materials in a warehouse; 10. a controlled feed pulverizer; 11. an integrated circulating gas dryer; 12. a feed buffer; 13. a mechanical and pneumatic coupling type pulverized coal feeding device; 14. a pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid thermal cracking reaction zone; 15. a mixed fluid temperature control zone; 16. a vortex flow field transfer zone; 17. a mixed fluid rectification zone; 18. preparing a hydrogen-rich gas reaction area by secondary cracking of the circulating particles; 19. a coal tar pretreatment subsystem; 20. a raw oil fraction cutting subsystem; 21. a distillate oil hydrogenation upgrading subsystem; 22. a product separation and recovery subsystem; 23. an oil storage subsystem; 24. a washing and purifying subsystem; 25. a molecular sieve adsorption subsystem; 26. a light component purification and separation subsystem; 27. a methane separation and purification subsystem; 28. a cryogenic liquefaction subsystem; an LNG storage subsystem; 30. a raw material gas component regulation subsystem; 31. a raw gas purification subsystem; 32. a low-carbon alcohol synthesis reaction subsystem; 33. a low-carbon mixed alcohol separation subsystem; 34. a product refining subsystem; 35. a lower alcohol storage subsystem; 36. oil-gas flow-dividing subsystem
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings.
Referring to fig. 1, the system comprises a system 1 for synchronously preparing methane-rich synthesis gas and light coal tar, a coal tar deep conversion system 2 communicated with a coal tar outlet of the system 1 for synchronously preparing methane-rich synthesis gas and light coal tar, a methane enrichment separation and cryogenic liquefaction system 3 communicated with a methane-rich synthesis gas outlet of the system 1 for synchronously preparing methane-rich synthesis gas and light coal tar, and a low carbon alcohol synthesis system 4;
the system 1 for synchronously preparing the methane-rich synthesis gas and the light coal tar comprises a continuous pressurization steady-state feeding subsystem 5 and a pulverized coal rapid pressurization pyrolysis reaction subsystem 6 communicated with the continuous pressurization steady-state feeding subsystem 5, wherein a crude synthesis gas outlet of the pulverized coal rapid pressurization pyrolysis reaction subsystem 6 is connected with a particle sieve molecular system 7, an outlet at the upper end of the particle sieve molecular system 7 is connected with an oil-gas shunting subsystem 36, and an outlet at the lower end of the particle sieve molecular system 7 is connected with the pulverized coal rapid pressurization pyrolysis reaction subsystem 6 through a circulating particle control shunting subsystem 8;
the coal tar deep conversion system 2 comprises a coal tar pretreatment subsystem 19, a raw oil fraction cutting subsystem 20, a distillate oil hydrogenation upgrading subsystem 21, a product separation and recovery subsystem 22 and an oil product storage subsystem 23 which are sequentially connected, wherein the coal tar pretreatment subsystem 19 is communicated with a light coal tar outlet of an oil gas diversion subsystem 36;
the methane enrichment separation and cryogenic liquefaction system 3 comprises a washing and purification subsystem 24, a molecular sieve adsorption subsystem 25, a light component purification separation subsystem 26, a methane separation and purification subsystem 27, a cryogenic liquefaction subsystem 28 and an LNG storage subsystem 29 which are sequentially connected, wherein the washing and purification subsystem 24 is communicated with a methane-rich synthetic gas outlet of an oil-gas flow-dividing subsystem 36;
the low-carbon alcohol synthesis system 4 comprises a raw material gas component regulation and control subsystem 30, a raw material gas purification subsystem 31, a low-carbon alcohol synthesis reaction subsystem 32, a low-carbon mixed alcohol separation subsystem 33, a product refining subsystem 34 and a low-carbon alcohol storage subsystem 35 which are connected in sequence, wherein the raw material gas component regulation and control subsystem 30 is connected with an LNG storage subsystem 29 outlet of the methane enrichment separation and cryogenic liquefaction system 3.
The continuous pressurization steady-state feeding subsystem 5 comprises a raw material storage bin 9, a controllable feeding pulverizer 10, an integrated circulating gas dryer 11, a feeding buffer 12 and a mechanical pneumatic coupling type pulverized coal feeding device 13 which are sequentially connected, wherein the mechanical pneumatic coupling type pulverized coal feeding device 13 is communicated with the coal rapid pressurization thermal cracking reaction subsystem 6.
The coal rapid pressurization and pyrolysis reaction subsystem 6 comprises a pulverized coal constant-temperature pressurization-catalytic hydrogenation rapid thermal cracking reaction area 14, a mixed fluid temperature control area 15, a vortex flow field transmission area 16, a mixed fluid rectification area 17 and a reaction area 18 for preparing hydrogen-rich gas by secondary cracking of circulating particles, which are sequentially connected from top to bottom and can realize internal material and energy coupling, wherein the vortex flow field transmission area 16 is connected with a mechanical pneumatic coupling type pulverized coal feeding device 13 of the coal rapid pressurization and pyrolysis reaction subsystem 6, a methane-rich synthetic gas outlet of the pulverized coal constant-temperature pressurization-catalytic hydrogenation rapid thermal cracking reaction area 14 is connected with a particle sieve molecular system 7, a gas outlet of the particle sieve molecular system 7 is connected with a methane enrichment separation and washing and purifying subsystem 24 of the cryogenic liquefaction system 3, and a hydrogen gas outlet at the lower end of the particle sieve molecular system 7 returns to the circulating particle secondary cracking reaction area through a circulating particle control shunting subsystem 8 to prepare hydrogen-rich reverse cracking gas Zone 18 is used to produce hydrogen-rich syngas.
The particle sieve molecular system 7 is used for grading, segmenting, classifying and recycling inert particles with the particle size of 50-600 mu m and carbon-rich particles with the fixed carbon content of 60-80 wt% and the particle size of less than 50 mu m.
The circulating particle control and shunting subsystem 8 is coupled with an external grading and sectional material returning system through an internal multi-channel particle circulating device, and forms a circulating flux of 1000-5000 kg/m based on a local jet flow configuration in the reactor 2 S high rate particle cycle with 10-20MJ/m 2 S heat flux of 1 to 10ms, 10 3 ～10 5 And instantaneously heating the pulverized coal to the pyrolysis temperature of 500-700 ℃ at the temperature rise rate of K/s.
The composition of the methane-rich synthesis gas output by the oil-gas diversion subsystem 36 is CO 30-41 vol%, and H 2 6～30vol％CH 4 8～30vol％，C m H n 0.1～0.2vol％CO 2 18～27vol％，N 2 2～5vol％。
The circulating particle control flow-dividing subsystem 8 adopts water vapor and CO 2 One or two of synthetic gas, air, oxygen-enriched gas or pure oxygenActivating the captured inert particles by the activating gas prepared according to any proportion, increasing the number of mesopores and micropores in the inert particles and improving the pore structure and surface active sites in the particles by the activating gas;
the operation pressure of the pulverized coal rapid pressurization and thermal cracking reaction subsystem 6 is 3.0-7.0 MPa, the reaction temperature range of the reaction zone 18 for preparing the hydrogen-rich gas by secondary cracking of circulating particles is 950-1200 ℃, and the reaction temperature range of the reaction zone 14 for the pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid thermal cracking reaction zone is 500-700 ℃.
The raw material gas component regulates and controls the hydrogen-carbon ratio H of the low-carbon alcohol synthesis raw material gas output by the subsystem 30 2 /CO＝2.10～4.8；
The final output product of the low-carbon alcohol synthesis system 4 comprises the following components: 30-75 wt% of methanol, 8-13 wt% of ethanol, 2-10 wt% of propanol, 5-15 wt% of butanol/isobutanol, and C + 5 2-5 wt% of alcohol.
The yield of light oil of the invention is 10-25 wt%; the circulating particle secondary cracking hydrogen production unit comprises a particle heating and activating area, a primary cracking reaction area and a deep cracking reaction area;
referring to fig. 1, the method for preparing LNG from coal and co-producing low carbon alcohol and fuel oil according to the present invention comprises the following steps:
firstly, raw material coal in a raw material storage bin 9 in a system 1 for synchronously preparing methane-rich synthesis gas and light coal tar is crushed into pulverized coal particles with the particle size of 10-1000 mu m by a controllable feeding crusher 10, then the pulverized coal with the water content lower than 2.0 wt% is dried by an integrated circulating gas dryer 11 and enters a feeding buffer 12, then the pulverized coal particles are conveyed to a vortex flow field transfer area 16 of a pulverized coal rapid pressurization and pyrolysis reaction subsystem 6 by a mechanical-pneumatic coupling type pulverized coal feeding device 13, a hydrogen-rich high-temperature gas-solid mixed heat carrier obtained by a reaction area 18 for preparing hydrogen-rich gas by secondary pyrolysis of the circulating particles and inert particles returned by a built-in multi-channel material returning system are uniformly mixed in a mixed fluid rectifying area 17, the temperature is reduced to about 600 ℃, the mixture continuously ascends into the vortex flow field transfer area 16 to be mixed with fresh pulverized coal and then ascends at a high speed to enter a mixed fluid temperature control area 15 to finish rapid heat transfer, after being heated to the preset pyrolysis temperature of 550-600 ℃, the pulverized coal continues to ascend and enters a pulverized coal constant-temperature pressurizing and catalytic hydrogenation rapid pyrolysis reaction zone 14 for pyrolysis;
secondly, the coal dust particles are converted into tar steam, methane, CO and H by a one-step method in a system 1 for synchronously preparing the methane-rich synthesis gas and the light coal tar 2 、CO 2 And a small amount of other components, the particles with different attributes in the raw synthesis gas are collected by a particle sieve molecular system 7 and then returned to different reaction areas of a pulverized coal rapid pressurization thermal cracking reaction subsystem 6 through a circulating particle control shunting subsystem 8 in a grading, segmenting and classifying manner, wherein the carbon-rich particles are circularly returned to the circulating particle secondary cracking to prepare a hydrogen-rich gas reaction area 18 for preparing hydrogen-rich synthesis gas, the hydrogen-rich gas is used as a hydrogen source for the hydro-pyrolysis of a pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid thermal cracking reaction area 14, and the methane-rich synthesis gas and the products output by the light coal tar system 1 are respectively liquid high-quality medium-low temperature coal tar and gaseous methane-rich synthesis gas;
then, the product of the pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid thermal cracking reaction zone 14 of the pulverized coal rapid pressurization thermal cracking reaction subsystem 6 is sent to an oil-gas distribution subsystem 36 after passing through a particle sieve molecular system 7, and low-temperature coal tar distributed by the oil-gas distribution subsystem enters a coal tar pretreatment subsystem 19 of a coal tar deep conversion system 2 at the downstream for dust removal, dehydration, desalination and purification, and then enters a raw oil fraction cutting subsystem 20 for cutting the purified coal tar into light distillate, middle distillate and heavy distillate; the distillate oil with different distillation ranges enters a subsequent distillate oil hydrogenation upgrading subsystem 21 to be finally converted into clean fuel oil products with high added values and fine chemical products, and the clean fuel oil products and the fine chemical products are sent to an oil product storage subsystem 23;
the methane-rich synthetic gas after the recovery and dust removal purification treatment of the medium and low temperature coal tar is used for removing CO in the synthetic gas from the oil gas diversion subsystem 36 to the washing and purification subsystem 24 of the methane enrichment separation and cryogenic liquefaction system 3 2 、H 2 S, COS and other acidic gas impurities enter the molecular sieve adsorption subsystem 25 for deep purification and removal of CH in the synthesis gas 3 OH、H 2 O、CO 2 The trace impurities are equal to obtain the main component H 2 、CO、CH 4 The methane-rich purified synthesis gas enters a subsequent light component purification and separation subsystem 26, a methane separation and purification subsystem 27 and a cryogenic liquefaction subsystem 28, and the finally produced LNG product with the methane concentration of more than 97 vol% is sent to an LNG storage subsystem 29;
finally, the CH is removed from the LNG storage subsystem 29 of the methane enrichment separation and cryogenic liquefaction system 3 4 The synthesis gas enters a raw material gas component regulation subsystem 30 of a downstream low-carbon alcohol synthesis system 4 to regulate the hydrogen-carbon ratio in the synthesis gas to 2.10-4.8, and the synthesis gas after the hydrogen-carbon ratio regulation enters a raw material gas purification subsystem 31 to remove CO 2 、H 2 And O and the like, and the output qualified raw material gas enters the low-carbon alcohol synthesis reaction subsystem 32, and the low-carbon mixed alcohol produced by the low-carbon alcohol synthesis reaction subsystem 32 passes through the low-carbon mixed alcohol separation subsystem 33 and the product refining subsystem 34 in sequence and then is sent to the low-carbon alcohol storage subsystem 35.
Claims (10)
1. The utility model provides a system of coal system LNG coproduction low carbon alcohol, fuel oil which characterized in that: the method comprises a system (1) for synchronously preparing the methane-rich synthesis gas and the light coal tar, a coal tar deep conversion system (2) communicated with a coal tar outlet of the system (1) for synchronously preparing the methane-rich synthesis gas and the light coal tar, a methane enrichment separation and cryogenic liquefaction system (3) communicated with a methane-rich synthesis gas outlet of the system (1) for synchronously preparing the methane-rich synthesis gas and the light coal tar, and a low carbon alcohol synthesis system (4);
the system (1) for synchronously preparing the methane-rich synthesis gas and the light coal tar comprises a continuous pressurization steady-state feeding subsystem (5) and a pulverized coal rapid pressurization thermal cracking reaction subsystem (6) communicated with the continuous pressurization steady-state feeding subsystem, wherein a crude synthesis gas outlet of the pulverized coal rapid pressurization thermal cracking reaction subsystem (6) is connected with a particle screening subsystem (7), an outlet at the upper end of the particle screening subsystem (7) is connected with an oil-gas shunting subsystem (36), and an outlet at the lower end of the particle screening subsystem (7) is connected with the pulverized coal rapid pressurization thermal cracking reaction subsystem (6) through a circulating particle control shunting subsystem (8);
the coal tar deep conversion system (2) comprises a coal tar pretreatment subsystem (19), a raw oil fraction cutting subsystem (20), a distillate oil hydrogenation upgrading subsystem (21), a product separation and recovery subsystem (22) and an oil product storage subsystem (23) which are sequentially connected, wherein the coal tar pretreatment subsystem (19) is communicated with a light coal tar outlet of an oil gas diversion subsystem (36);
the methane enrichment separation and cryogenic liquefaction system (3) comprises a washing and purifying subsystem (24), a molecular sieve adsorption subsystem (25), a light component purification and separation subsystem (26), a methane separation and purification subsystem (27), a cryogenic liquefaction subsystem (28) and an LNG storage subsystem (29) which are sequentially connected, wherein the washing and purifying subsystem (24) is communicated with a methane-rich synthetic gas outlet of an oil-gas shunting subsystem (36);
the low-carbon alcohol synthesis system (4) comprises a raw material gas component regulation and control subsystem (30), a raw material gas purification subsystem (31), a low-carbon alcohol synthesis reaction subsystem (32), a low-carbon mixed alcohol separation subsystem (33), a product refining subsystem (34) and a low-carbon alcohol storage subsystem (35) which are sequentially connected, wherein the raw material gas component regulation and control subsystem (30) is connected with an LNG (liquefied natural gas) storage subsystem (29) outlet of the methane enrichment separation and cryogenic liquefaction system (3);
raw material coal in a raw material storage bin (9) in a system (1) for synchronously preparing methane-rich synthesis gas and light coal tar is crushed into pulverized coal particles with the particle size of 10-1000 mu m by a controllable feeding crusher (10), the pulverized coal dried by an integrated circulating gas dryer (11) until the water content is lower than 2.0 wt% enters a feeding buffer (12), then the pulverized coal is conveyed to a vortex flow field transfer area (16) of a pulverized coal rapid pressurization pyrolysis reaction subsystem (6) by a mechanical and pneumatic coupling type pulverized coal feeding device (13), a hydrogen-rich high-temperature gas-solid mixed heat carrier obtained by preparing a hydrogen-rich gas reaction area (18) from the secondary pyrolysis of circulating particles and inert particles returned by a built-in multichannel return system are uniformly mixed in a mixed fluid rectifying area (17), the temperature is reduced to 600 ℃, the inert particles continuously flow upwards into the vortex flow field transfer area (16) to be mixed with fresh pulverized coal and then flow upwards at a high speed to enter a mixed fluid temperature control area (15) to finish rapid heat transfer, the pulverized coal is heated to the preset pyrolysis temperature of 550-600 ℃, and then continuously ascends to enter a pulverized coal constant-temperature-pressurization-catalytic hydrogenation rapid pyrolysis reaction zone (14) for pyrolysis.
2. The system for co-production of low carbon alcohol and fuel oil product from coal-based LNG as claimed in claim 1, wherein: the continuous pressurization steady-state feeding subsystem (5) comprises a raw material storage bin (9), a controllable feeding crusher (10), an integrated circulating gas dryer (11), a feeding buffer (12) and a mechanical pneumatic coupling type pulverized coal feeding device (13) which are sequentially connected, wherein the mechanical pneumatic coupling type pulverized coal feeding device (13) is communicated with the coal rapid pressurization thermal cracking reaction subsystem (6).
3. The system for co-production of low carbon alcohol and fuel oil product from coal-based LNG as claimed in claim 1, wherein: the pulverized coal rapid pressurization and pyrolysis reaction subsystem (6) comprises a pulverized coal constant-temperature pressurization-catalytic hydrogenation rapid pyrolysis reaction region (14), a mixed fluid temperature control region (15), a vortex flow field transfer region (16), a mixed fluid rectification region (17) and a circulating particle secondary pyrolysis hydrogen-rich gas preparation reaction region (18) which are sequentially connected and communicated from top to bottom, and can realize internal material and energy coupling, wherein the vortex flow field transfer region (16) is connected with a mechanical pneumatic coupling type pulverized coal feeding device (13) of the pulverized coal rapid pressurization and pyrolysis reaction subsystem (6), a methane-rich synthetic gas outlet of the pulverized coal constant-pressure-catalytic hydrogenation rapid pyrolysis reaction region (14) is connected with a particle sieve molecular system (7), and a lower end outlet of the particle sieving subsystem (7) returns to the circulating particle secondary pyrolysis hydrogen-rich gas preparation reaction region (18) through a circulating particle control shunt subsystem (8) and is used for preparing the hydrogen-rich synthetic hydrogen-rich gas And (4) qi.
4. The system for co-production of low-carbon alcohol and fuel oil by coal LNG as claimed in claim 1, wherein the particle sieving subsystem (7) is used for grading, segmenting and classifying the inert particles with the particle size of 50-600 μm and the carbon-rich particles with the fixed carbon content of 60-80 wt% and the particle size of less than 50 μm for recycling.
5. The system for co-production of low carbon alcohol and fuel oil product from coal-based LNG as claimed in claim 1, wherein: the circulating particle control shunting subsystem (8) is internally provided with a multi-channel particle circulating device and externally provided with a particle circulating deviceThe coupling of a grading and sectional material returning system forms 1000-5000 kg/m of circulating flux based on the local jet flow configuration in the reactor 2 S high rate particle cycle with 10-20MJ/m 2 S heat flux of 1 to 10ms, 10 3 ～10 5 And instantaneously heating the pulverized coal to the pyrolysis temperature of 500-700 ℃ at the temperature rise rate of K/s.
6. The system for CO-production of low carbon alcohol and fuel oil by coal LNG as claimed in claim 1, wherein the composition of the methane-rich syngas output by the oil-gas split-flow subsystem (36) is CO 30-41 vol%, and H is H 2 6～30vol％，CH 4 8～30vol％，C m H n 0.1～0.2vol％， CO 2 18～27vol％，N 2 2～5vol％。
7. The system for CO-production of low carbon alcohol and fuel oil by coal LNG as claimed in claim 1, wherein the circulating particle control sub-system (8) employs steam and CO 2 And one or more than two of synthetic gas, air, oxygen-enriched gas or pure oxygen are prepared into activating gas according to any proportion to activate the captured inert particles.
8. The system for co-production of low carbon alcohol and fuel oil by coal LNG as claimed in claim 1, wherein the operating pressure of the pulverized coal rapid pressurization thermal cracking reaction subsystem (6) is 3.0-7.0 MPa, the reaction temperature range of the reaction zone (18) for preparing hydrogen-rich gas by secondary cracking of circulating particles is 950-1200 ℃, and the reaction temperature range of the pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid thermal cracking reaction zone (14) is 500-700 ℃.
9. The system for co-production of low carbon alcohol and fuel oil product from coal-based LNG as claimed in claim 1, wherein: the raw material gas component regulates and controls the hydrogen-carbon ratio H of the low-carbon alcohol synthesis raw material gas output by the subsystem (30) 2 /CO＝2.10～4.8；
The final output product of the low-carbon alcohol synthesis system (4) comprises the following components: 30-75 wt% of methanol and 8-c of ethanol13 wt%, 2-10 wt% of propanol, 5-15 wt% of butanol/isobutanol, and C + 5 2-5 wt% of alcohol and one hundred percent of each component of the product.
10. A method for coproducing low-carbon alcohol and fuel oil from coal-based LNG is characterized by comprising the following steps: firstly, raw material coal in a raw material storage bin (9) in a system (1) for synchronously preparing methane-rich synthesis gas and light coal tar is crushed into pulverized coal particles with the particle size of 10-1000 mu m by a controllable feeding crusher (10), the pulverized coal with the water content of less than 2.0 wt% is dried by an integrated circulating gas dryer (11) and enters a feeding buffer (12), then the pulverized coal is conveyed to a vortex flow field transfer region (16) of a pulverized coal rapid pressurization pyrolysis reaction subsystem (6) by a mechanical-pneumatic coupling pulverized coal feeding device (13), hydrogen-rich high-temperature gas-solid heat carrier mixed from a reaction region (18) for preparing hydrogen-rich gas by secondary pyrolysis of circulating particles and inert particles returned by a built-in multi-channel return system are uniformly mixed in a mixed fluid rectifying region (17), the temperature is reduced to 600 ℃, the mixture continuously ascends to the vortex flow field transfer region (16) and enters a mixed fluid temperature control region (15) at high speed after being mixed with fresh pulverized coal to finish rapid heat transfer, after being heated to the preset pyrolysis temperature of 550-600 ℃, the pulverized coal continuously ascends to enter a pulverized coal constant-temperature-pressurization-catalytic hydrogenation rapid pyrolysis reaction zone (14) for pyrolysis;
secondly, the coal dust particles are converted into tar steam, methane, CO and H by a one-step method in a system (1) for synchronously preparing the methane-rich synthesis gas and the light coal tar 2 、CO 2 And a small amount of other components, the particles with different attributes in the raw synthesis gas are collected by a particle screening subsystem (7) and then returned to different reaction areas of a pulverized coal rapid pressurization thermal cracking reaction subsystem (6) in a grading, segmentation and classification manner by a circulating particle control shunting subsystem (8), wherein the carbon-rich particles are circularly returned to the circulating particles for secondary cracking to prepare a hydrogen-rich gas reaction area (18) for preparing hydrogen-rich synthesis gas, the hydrogen-rich gas is used as a hydrogen source for the hydropyrolysis of a pulverized coal constant temperature-pressurization-catalytic hydrogenation rapid thermal cracking reaction area (14), and the methane-rich synthesis gas and products output by a light coal tar system (1) are respectively liquid high-quality medium-low temperature coal tar and gaseous methane-rich synthesis gasForming gas;
then, the product of the pulverized coal constant-temperature, pressurizing and catalytic hydrogenation rapid thermal cracking reaction area (14) of the pulverized coal rapid pressurizing thermal cracking reaction subsystem (6) is sent into an oil-gas distribution subsystem (36) after passing through a particle screening subsystem (7), and low-temperature coal tar distributed by the oil-gas distribution subsystem enters a coal tar pretreatment subsystem (19) of a coal tar deep conversion system (2) at the downstream for dust removal, dehydration, desalination and purification, and then enters a raw oil fraction cutting subsystem (20) for cutting the purified coal tar into light distillate, medium distillate and heavy distillate; the distillate oil with different distillation ranges enters a subsequent distillate oil hydrogenation upgrading subsystem (21) to be finally converted into clean fuel oil with high added value and fine chemical products, and the clean fuel oil and the fine chemical products are sent to an oil storage subsystem (23);
the methane-rich synthetic gas after the recovery and dust removal purification treatment of the medium and low temperature coal tar is used for removing CO in the synthetic gas from the oil gas diversion subsystem (36) to the washing and purifying subsystem (24) of the methane enrichment separation and cryogenic liquefaction system (3) 2 、H 2 S, COS acid gas impurity enters a molecular sieve adsorption subsystem (25) for deep purification and removal of CH in the synthesis gas 3 OH、H 2 O、CO 2 Trace impurities to obtain H as main component 2 、CO、CH 4 The methane-rich purified synthesis gas enters a subsequent light component purification and separation subsystem (26), a methane separation and purification subsystem (27) and a cryogenic liquefaction subsystem (28), and finally the produced LNG product with the methane concentration of more than 97 vol% is sent to an LNG storage subsystem (29);
finally, the decarbonization output by the LNG storage subsystem (29) of the methane enrichment separation and cryogenic liquefaction system (3) 4 The synthesis gas enters a raw material gas component regulation subsystem (30) of a downstream low-carbon alcohol synthesis system (4) to regulate the hydrogen-carbon ratio in the synthesis gas to 2.10-4.8, and the synthesis gas after the hydrogen-carbon ratio regulation enters a raw material gas purification subsystem (31) to remove CO 2 、H 2 And O impurities, namely the output qualified raw material gas enters a low-carbon alcohol synthesis reaction subsystem (32), and the low-carbon mixed alcohol produced by the low-carbon alcohol synthesis reaction subsystem (32) sequentially passes through a low-carbon mixed alcohol separation subsystem (33) and a product refining subsystem (34) and then is sent to a low-carbon alcohol storage subsystem (35).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710388523.1A CN107189803B (en) | 2017-05-27 | 2017-05-27 | System and method for co-production of low-carbon alcohol and fuel oil product by coal-based LNG (liquefied Natural gas) |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710388523.1A CN107189803B (en) | 2017-05-27 | 2017-05-27 | System and method for co-production of low-carbon alcohol and fuel oil product by coal-based LNG (liquefied Natural gas) |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107189803A CN107189803A (en) | 2017-09-22 |
| CN107189803B true CN107189803B (en) | 2022-09-16 |
Family
ID=59874643
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710388523.1A Active CN107189803B (en) | 2017-05-27 | 2017-05-27 | System and method for co-production of low-carbon alcohol and fuel oil product by coal-based LNG (liquefied Natural gas) |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107189803B (en) |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101735008B (en) * | 2009-12-07 | 2013-08-14 | 中国科学院山西煤炭化学研究所 | Technology for co-producing low-carbon alcohol and natural gas by coal synthesis gas |
| CN102061182B (en) * | 2011-01-19 | 2013-01-09 | 北京华福工程有限公司 | Method for coal hydrogenation pyrolysis and gasification coupling |
| CN104832226B (en) * | 2015-03-31 | 2016-08-24 | 李大鹏 | A kind of coal liquifaction and coal gas power generating simultaneously device and method |
| CN105037086B (en) * | 2015-07-31 | 2017-12-15 | 赛鼎工程有限公司 | A kind of Multi-class propagation technique through preparing low-carbon mixed alcohol by synthetic gas by coal |
| CN105152859B (en) * | 2015-07-31 | 2017-09-19 | 赛鼎工程有限公司 | Coke-stove gas produces low-carbon alcohols and the technique of by-product natural gas with synthesis gas |
-
2017
- 2017-05-27 CN CN201710388523.1A patent/CN107189803B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN107189803A (en) | 2017-09-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102191086B (en) | Integration device and method for coproducing carbon monoxide, methanol, hydrogen and refined synthetic gas in process of producing synthetic gas from coal | |
| AU2009301573B2 (en) | Method and equipment for multistage liquefying of carbonaceous solid fuel | |
| CN103694074B (en) | System and process for preparing olefin by taking coal and coke-oven gas as raw materials | |
| CN103992823B (en) | Low-order coal and the method and system that biomass are Material synthesis methane and petrol and diesel oil | |
| CN103160294A (en) | Omnibearing coproduction system and method by utilizing coal grading | |
| CN103588221B (en) | A kind of coke(oven)gas produces method and the device of synthetic ammonia coproducing LNG | |
| CN102660330A (en) | Method for co-producing various chemical products by taking coal, petroleum, natural gas and salt as raw materials | |
| CN110862839B (en) | System and method for co-production of methanol from coal-based natural gas | |
| CN105779046A (en) | Method for preparing LNG (Liquefied Natural Gas) by using Fischer-Tropsch synthesis tail gas as raw material | |
| CN102041019A (en) | Method for coproducing substitute natural gas through coal liquefaction | |
| CN104974014A (en) | Production method for methanol | |
| CN102557869A (en) | Method for preparing methanol fuel by utilizing biomass charcoal | |
| CN102180767A (en) | Method and device for jointly producing methanol, ammonia and acetic acid by using coal and natural gas | |
| CN107189803B (en) | System and method for co-production of low-carbon alcohol and fuel oil product by coal-based LNG (liquefied Natural gas) | |
| CN105016297B (en) | A kind of preparation method of synthesis gas | |
| CN105111107B (en) | A kind of technique of coal low-carbon alcohols and Utilization of Carbon Dioxide | |
| CN107417495A (en) | A kind of ammonia from coal, LNG, the Poly-generation method and device of liquid fuel | |
| CN104986732A (en) | Method for preparing synthesis gas through coke oven gas and coal gas | |
| CN105152864A (en) | Technology for producing low carbon alcohol as well as by-product natural gas and liquefied ammonia from coke oven gas and synthetic gas | |
| CN202744473U (en) | Poly-generation device for producing olefin by taking coal and natural gas as raw materials | |
| CN110055106A (en) | A kind of method that low-order coal sub-prime prepares methanol and oil using Poly-generation | |
| CN105061264A (en) | Method for production of low carbon alcohol and combined production of natural gas and urea from synthetic gas and coke oven gas | |
| CN104945229B (en) | A kind of method for producing dimethyl ether | |
| CN207175869U (en) | A kind of coal LNG coproduction low-carbon alcohols, the system of fuel oil | |
| CN203639364U (en) | System for preparing olefin by taking coal and coke-oven gas as raw materials |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |