CN101709227B - Comprehensive method and system for utilizing carbon-contained organic matter - Google Patents
Comprehensive method and system for utilizing carbon-contained organic matter Download PDFInfo
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- CN101709227B CN101709227B CN200910177227.2A CN200910177227A CN101709227B CN 101709227 B CN101709227 B CN 101709227B CN 200910177227 A CN200910177227 A CN 200910177227A CN 101709227 B CN101709227 B CN 101709227B
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Classifications
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- 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
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
-
- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0979—Water as supercritical steam
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- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1659—Conversion of synthesis gas to chemicals to liquid hydrocarbons
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- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1662—Conversion of synthesis gas to chemicals to methane
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
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Abstract
The invention relates to a comprehensive method for utilizing a carbon-contained organic matter, comprising a high-pressure hot water/supercritical water gasifying sub-method and a poly-generation sub-method, wherein the high-pressure hot water/supercritical water gasifying sub-method is continuously carried out by the decompression continuous discharge of a reaction product. The decompression continuous discharge is realized by adopting at least two buffer tanks which are operated in parallel connection or at least one decompressing valve. The invention converts the carbon-contained organic matter into a clean energy chemical product, such as methane, and the like and/or clean electricity by coupling the high-pressure hot water/supercritical water gasifying sub-method, the poly-generation sub-method, an alga carbon absorbing sub-method and/or a composite energy source hydrogen preparation sub-method to form an ecological cycle mode for the development and utilization of carbon-contained organic matter resources. The invention also provides a comprehensive system for implementing the comprehensive method.
Description
Invention field
The present invention relates to Coal Chemical Industry, more specifically, the present invention relates to high-pressure water heating/supercritical water gasification submethod and to be coupled with other method the integrated approach utilizing carbon-contained organic matter and the system implementing this integrated approach.
Background technology
The bottleneck problem of shortage of resources and environmental pollution is two large hot issues of the world today.Along with Economic development and industrial progress, the continuous quickening of urbanization process and the raising of people's material life, demand sustainable growth on the one hand to the disposable energy, the quantity of organic waste as trade waste and urban life refuse also increases sharply on the other hand, causes the huge waste of resource.And new energy technology not only technically but also will will can meet the growing economy development requirement of the mankind in standing stock, more the mankind to be met and the Nature develops in harmony to the requirement of environment.Therefore, the coal resources of rich reserves, reproducible biomass energy and organic waste being converted into clean, efficient high heating value gaseous fuel, is the only way which must be passed seeking Energy efficiency, economic benefit and environmental benefit harmony.
Coal plays very important role in mankind's energy resource supply always.Even if during the third generation energy based on oil, in world's Energy Mix, coal still occupies the ratio of 27%.At present, Coal Gasification Technology is varied in the world, and the coal that often kind of coal gasification method is suitable for is each different.Typical large-scale coal gasifying process mainly comprises fixed bed crushed coal pressure gasifying technique, Texaco's slurry pressure gasification process and shell dry coal powder pressure gasifying technique.The current representational industrialization gasification type of furnace has: fixed bed gasification (Lurgi stove, BGL stove); Fluidized-bed gasification (Winkler stove, HTW stove, U-Gas stove, KRW stove and CFB vapourizing furnace); Entrained flow gasification (KT stove, Texaco stove, Shell stove, Prenflo stove and GSP stove).
But the coal gas that above-mentioned traditional method is obtained, its calorific value is only equivalent to the level of industrial gas, and its ultimate principle is to improve based on service temperature and pressure and the structure that improves equipment, the gas making efficiency of raising process that therefore can only be comparatively limited and the calorific value of coal gas.And be conducive to the condition of methane generation, except pressurization, the temperature of reaction that main needs are lower, as 700 DEG C, and aforesaid method needs more than 1000 DEG C usually, even up to 1800 DEG C, forms the gasification condition of slag tap.Traditional method need drying, empty point, gasification, aqueous vapor conversion, low-temperature rectisol, if produce methane, also need methanation workshop section, complex process, efficiency are low and invest huge.
Traditional biomass and organic waste produce combustion gas, usually adopt the mode of gasification.Steam gasification only has the temperature of water vapour to reach more than 700 DEG C, and gasification result is just more satisfactory, and this proposes higher requirement to vapour generator performance.Under normal circumstances, because steam gasification is difficult to reach higher temperature, therefore gas yield is lower.The Technology of partial oxidation, not only makes catalytic unit between 900 ~ 1400 DEG C, complete organic gasification.The height of temperature uses oxygen or air when depending on gasification.This Technology, except needing very high temperature, also can generate more pitch class synthetic.Burning and pyrolysis separate by two fluidized bed gasification, and combustion gas quality is better, and does not need extra thermal source and oxygen generating plant, and running cost is lower.But, due to thermal barrier quantitatively with the restriction of temperature, organic vaporization rate is lower.And the exhaust temperature that burning bed is discharged is higher, heat enthalpy value is higher, need to reclaim, otherwise waste is comparatively large, thus needs good waste-heat recovery device.On the other hand, because coke and thermal barrier circulate all at higher temperatures when running, be difficult to fixing quantity, more easily cause fluctuations and the instability of furnace temperature, therefore need the heating unit of assisting.
Utilizing the characteristic of high-pressure water heating and supercritical water carbon-contained organic matter to be converted into the inflammable gas such as hydrogen, methane is an emerging technology.Launch in the research in this field both at home and abroad, but present research is also in laboratory stage substantially.
Although high-pressure water heating and supercritical water are the effective means realizing organic recycling, but in sum, no matter be coal, biomass or be that organic waste transform and will realize industrialization and also there are some technical problems in high-pressure water heating and supercritical water, except equipment corrosion factor, the most thorny no more than blockage problem, when especially processing high concentration slurry, system often can not sustained continuous be run.And high density charging is significantly to realizing industrialization, can water loss be reduced on the one hand, reducing system energy consumption, be conducive to producing the gas being rich in methane on the other hand.
General Atomics company of the U.S. adopts the organic waste slurry of 40% to carry out supercritical water oxidation or gasification hydrogen-producing, but experimental result shows that high concentration slurry easily produces coking and blocking.High pressure water repercussion study is engaged in U.S.'s northwest Pacific laboratory (PNNL) for many years, is raw material mainly with fluid organic material.CCUJ company of Japan is that catalyzer carries out supercritical water gasification to coal with CaO, but CaO consumption is very large, brings solid waste disposal problem, is unsuitable for suitability for industrialized production.Karlsruhe, Germany research centre establishes a set of biomass supercritical water gasification device up to now maximum in the world, employing gas-fired is heated, treatment capacity 100L/h, although its target product is methane, final acquisition be but hydrogen-rich gas, in addition, even if when biomass concentration is lower (< 8%), this device still fails to solve thorny residual Jiao, tar, inorganic salt separate out the blockage problem caused.Xi'an Communications University is studied in gasifying biomass and coal and biomass altogether gasification.Guo Liejin etc. in its patent CN1654313A to biomass model and multiple biomass and coal gasification altogether in supercritical water, be that SOLID ORGANIC raw material carries out supercritical water gasification hydrogen production with sawdust in its patent CN1223508C, all adopt traditional electrical heating means, but the concentration very low (< 2wt%) of solid organic matters in experiment, and adopt lp piston to enter slurry, charging continuity is poor, is unfavorable for Product management model.The people such as Guo Liejin continue in patent CN101058404A, have studied biomass supercritical water fluid bed partial oxidation hydrogen making, still there is the on the low side and feed problems of slurry concentration, be unfavorable for that long-time continuous operates, be more unfavorable for the macromole biomass continuous gasification that ash content is higher.Extensive work has been made in low-rank coal supercritical water gasification hydrogen production aspect, coalification place, Shanxi.Bi Ji really waits people in its patent CN1219852C, disclose the method for low-rank coal continuous hydrogen production in subcritical water and supercritical water, adopt electrical heating method, enter to starch concentration up to 40%, but from related experiment result, the flow velocity of water is much larger than flow rate of slurry, and therefore in system, real water coal, than very large, is less than 10% according to its slurry actual concentrations of calculating, and unresolved blocking and continuous discharging slag problem, long-play risk is larger.
Visible, blocking of the prior art and the continuous discharging slag problems affect continuity of technique, people or have to carry out discontinuous operation to process high concentration slurry, or have to reduce slurry concentration in the hope of continuous running.Therefore, for the efficiency of industrial applications and the consideration of economy, people are exploring always and how to process continuously high concentration slurry, and this is also the problem that the present invention endeavours to solve.
After the gas products obtained after high-pressure water heating and supercritical water treatment at carbon-contained organic matter isolates methane, still have synthetic gas to exist, still need to utilize with methanol, ethylene glycol, low-carbon alcohol or dme etc. further it.Simultaneity factor also can produce carbonic acid gas, and Carbon emission on the impact of Global climate change by the world is paid close attention to, so need to solve the emission problem of carbonic acid gas.
When producing firedamp by syngas, methyl alcohol, ethylene glycol, low-carbon alcohol or dme etc., usually need to regulate ratio of carbon-hydrogen (as added a certain amount of hydrogen or supplementary carbon monoxide in synthetic gas).The industrial hydrogen of about 96% derives from the fossil energies such as Sweet natural gas, oil and coal at present, but uses the production technology of fossil energy hydrogen manufacturing and technique can not solve Carbon emission problem, thus can not realize ecological circulation and produce.In other hydrogen producing technology, application is at present comparatively wide and the hydrogen production process of relative maturity comprises water electrolysis hydrogen producing, biological hydrogen production, bioelectrochemistry hydrogen manufacturing and PhotoelectrochemicalSystem System for Hydrogen Production etc.It is current most prospect and the most feasible technology that the electric energy (comprising sun power, wind energy etc.) utilizing renewable energy source to produce carrys out water electrolysis hydrogen producing as power, is called as the optimal path leading to hydrogen economy.
To sum up, the coal-based chemical industry Poly-generation technology that countries in the world are developed in succession does not all have system to consider Resources of Carbon Dioxide Utilizing question, how to control and to reduce coal at the carbonic acid gas transformed and produce in combustion processes, and by its recycling, becoming the matter of utmost importance of New Coal Chemical technical development.Although in view of the seriousness of " Greenhouse effect ", American-European countries begins one's study coal-based near zero release polygenerations systeme in recent years, but due to carbon dioxide chemistry stable in properties, this coal-based near zero release polygenerations systeme cannot realize carbon dioxide discharge-reduction in process of production, the method trapping and seal up for safekeeping can only be adopted to go to solve, and this method is with high costs, really can not reduce carbonic acid gas from amount, long-range it seems is only makeshift.Thoroughly to solve the problem of carbonic acid gas, just must break through the limitation of existing fossil energy, renewable energy source be introduced the production process of coal-based Chemicals, realize the fusion of multiple-energy-source, be derived energy chemical product by carbon dioxide conversion, thus realize the near zero release of production process carbonic acid gas.
Summary of the invention
The invention provides a kind of integrated approach utilizing carbon-contained organic matter, comprising:
High-pressure water heating/supercritical water gasification submethod and Poly-generation submethod, wherein said high-pressure water heating/supercritical water gasification submethod, comprising:
A) in reactor, the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product;
B) described reaction product decompressing and continuous is discharged in the first separator;
C) make reaction product in the first separator, carry out gas/liquid to be admittedly separated, obtain gaseous product and liquid-solid mixture, wherein gaseous product comprises inflammable gas, discharges this gaseous product; Liquid-solid mixture is then discharged in the second separator;
Gu d) carry out liquid/separation to liquid-solid mixture in the second separator, obtain product liquid and solid residue, and discharge continuously respectively.
In a preferred embodiment, method of the present invention also comprises algae suction carbon submethod.
In a preferred embodiment, method of the present invention also comprises compound energy hydrogen manufacturing submethod.
In a preferred embodiment, method of the present invention also comprises catalyzer, water or the steam reclaimed in described integrated approach, solid materials circulate it, and utilizes the waste heat in described integrated approach or top pressure power generation or produce steam.
Present invention also offers a kind of system ensemble utilizing carbon-contained organic matter, comprise high-pressure water heating/supercritical water gasification subsystem and Poly-generation subsystem, wherein said high-pressure water heating/supercritical water gasification subsystem comprises reactor, the first separator, the second separator, it is characterized in that between described reactor and the first separator and/or between the first separator and the second separator, be provided with the equipment can discharged for material decompressing and continuous.
In a preferred embodiment, system of the present invention also comprises algae suction carbon subsystem.
In a preferred embodiment, system of the present invention also comprises compound energy hydrogen manufacturing subsystem.
In a preferred embodiment, system of the present invention also comprise catalyzer, water or the steam reclaimed in described system ensemble, solid materials circulation device, and utilize the device of waste heat in described system ensemble or top pressure power generation or generation steam.
Accompanying drawing explanation
Fig. 1 is the first embodiment schematic diagram of high-pressure water heating/supercritical water gasification submethod.
Fig. 2 is the second embodiment schematic diagram of high-pressure water heating/supercritical water gasification submethod.
Fig. 3 is the 3rd embodiment schematic diagram of high-pressure water heating/supercritical water gasification submethod.
Fig. 4 is the 4th embodiment schematic diagram of high-pressure water heating/supercritical water gasification submethod.
Fig. 5 is the embodiment schematic diagram that high-pressure water heating of the present invention/supercritical water gasification submethod is combined with Poly-generation submethod.
The embodiment schematic diagram that Fig. 6 to be high-pressure water heating of the present invention/supercritical water gasification submethod with Poly-generation submethod, algae inhale carbon submethod and compound energy hydrogen manufacturing submethod are combined.
Another embodiment schematic diagram that Fig. 7 to be high-pressure water heating of the present invention/supercritical water gasification submethod with Poly-generation submethod, algae inhale carbon submethod and compound energy hydrogen manufacturing submethod are combined.
Embodiment
One. high-pressure water heating/supercritical water gasification submethod and subsystem
The application provides following submethod and subsystem:
1. high-pressure water heating/supercritical water gasification submethod, comprising:
A) in reactor (4), the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product;
B) described reaction product decompressing and continuous is discharged in the first separator (6);
C) make reaction product carry out gas/liquid in the first separator (6) to be admittedly separated, obtain gaseous product and liquid-solid mixture, wherein gaseous product comprises inflammable gas, discharges this gaseous product; Liquid-solid mixture is then discharged in the second separator (7);
D) at the second separator (7) Gu in liquid/separation is carried out to liquid-solid mixture, obtain product liquid and solid residue, and discharge respectively continuously.
2. according to above-mentioned 1 submethod, wherein carry out implementation step b by least two surge tanks be connected in parallel to each other (8) be positioned between reactor (4) and the first separator (6)), wherein under continuous duty, have at least a surge tank to be used for reception and carry out the reaction product of autoreactor (4), and have a surge tank at least for the reaction product received being discharged in the first separator (6).
3. according to above-mentioned 1 submethod, wherein carry out implementation step b by least one reducing valve (9) be positioned between reactor (4) and the first separator (6)).
4. high-pressure water heating/supercritical water gasification submethod, comprising:
A) in reactor (4), the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product;
B) make reaction product be discharged to the first separator (6) continuously, and in the first separator (6), carry out gas/liquid be admittedly separated, obtain gaseous product and liquid-solid mixture, wherein gaseous product comprises inflammable gas, discharges this gaseous product;
C) by step b) liquid-solid mixture decompressing and continuous be discharged in the second separator (7);
D) at the second separator (7) Gu in liquid/separation is carried out to described liquid-solid mixture, obtain product liquid and solid residue, and discharge respectively continuously.
5. according to above-mentioned 4 submethod, wherein carry out implementation step c by least two surge tanks be connected in parallel to each other (8) be positioned between the first separator (6) and the second separator (7)), wherein under continuous duty, have at least a surge tank to be used for receiving the liquid-solid mixture from the first separator (6), and have a surge tank at least for liquid-solid mixture being discharged to the second separator (7).
6. according to above-mentioned 4 submethod, wherein carry out implementation step c by least one reducing valve be positioned between the first separator (6) and the second separator (7)).
7. high-pressure water heating/supercritical water gasification submethod, comprising:
A) in reactor (4), the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product;
B) described reaction product decompressing and continuous is discharged in the first separator (6);
C) make reaction product carry out gas/liquid in the first separator (6) to be admittedly separated, obtain gaseous product and liquid-solid mixture, wherein gaseous product comprises inflammable gas, discharges this gaseous product;
D) by step c) liquid-solid mixture decompressing and continuous be discharged in the second separator (7);
E) at the second separator (7) Gu in liquid/separation is carried out to described liquid-solid mixture, obtain product liquid and solid residue, and discharge respectively continuously.
8. according to above-mentioned 7 submethod, wherein carry out implementation step b by least two surge tanks be connected in parallel to each other (8) be positioned between reactor (4) and the first separator (6)), wherein under continuous duty, have at least a surge tank to be used for reception and carry out the reaction product of autoreactor (4), and have a surge tank at least for the reaction product received being discharged in the first separator (6); And carry out implementation step d by least two surge tanks be connected in parallel to each other be positioned between the first separator (6) and the second separator (7)), wherein under continuous duty, have at least a surge tank to be used for receiving the liquid-solid mixture from the first separator (6), and have a surge tank at least for liquid-solid mixture being discharged to the second separator (7).
9. according to above-mentioned 7 submethod, wherein carry out implementation step b by least one reducing valve be positioned between reactor (4) and the first separator (6)), and wherein carry out implementation step d by least one reducing valve be positioned between the first separator (6) and the second separator (7)).
10. high-pressure water heating/supercritical water gasification submethod, comprising:
A) in reactor (4), the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product;
B) described reaction product decompressing and continuous is discharged in gas-liquid-solid three-phase separator (10);
C) make reaction product at gas-liquid-solid three-phase separator (10) Gu in carry out gas/liquid/separation, obtain gaseous product, product liquid and solid product, wherein gaseous product comprises inflammable gas, respectively continuous Exhaust Gas product, product liquid and solid product.
11. according to above-mentioned 10 submethod, wherein realize step b by least two surge tanks be connected in parallel to each other be positioned between reactor (4) and gas-liquid-solid three-phase separator (10)), wherein under continuous duty, have at least a surge tank to be used for reception and carry out the reaction product of autoreactor (4), and have a surge tank at least for the reaction product received being discharged in gas-liquid-solid three-phase separator (10).
12. according to above-mentioned 10 submethod, wherein realize step b by least one reducing valve (9) be positioned between reactor (4) and gas-liquid-solid three-phase separator (10)).
13. according to the above-mentioned submethod of 1,4,7 or 10, wherein also comprised before described step a) and described slurry is preheated to temperature required step with high temperature rise rate.
14. according to above-mentioned 13 submethod, wherein said high temperature rise rate is 30-50 DEG C/min.
15. according to above-mentioned 13 submethod, wherein said high temperature rise rate preheating by high-frequency electromagnetic heating, microwave heating or gas fuel burning heating realize.
16. according to the above-mentioned submethod of 1,4,7 or 10, and wherein said high concentration slurry comprises the carbon-contained organic matter of 10-60wt%, and wt% is based on slurry gross weight.
17. according to the above-mentioned submethod of 1,4,7 or 10, and wherein said high concentration slurry comprises the carbon-contained organic matter of 50-60wt%, and wt% is based on slurry gross weight.
18. according to the above-mentioned submethod of 1,4,7 or 10, and wherein said catalyzer is selected from following a few class: (I) basic metal or alkaline earth metal oxide, basic metal or alkaline earth salt or basic metal or alkaline earth metal hydroxides or their mixture; (II) one or more transition metal on carrier are carried on; (III) mineral substance of iron content.
19. according to above-mentioned 18 submethod, wherein said (I) class catalyzer is selected from K
2o, Na
2o, CaO, MgO, NaOH, KOH, Ca (OH)
2, Mg (OH)
2, K
2cO
3, Na
2cO
3or their mixture.
20. according to above-mentioned 18 submethod, wherein said (II) class catalyzer is selected from load Ni, Ru, Fe on carrier or K-Ni, K-Fe, K-Ni-Fe composite catalyst be carried on carrier.
21. according to above-mentioned 18 submethod, wherein said (III) class catalyzer is selected from Fe
3o
4, peridotites, rhombspar, rhombohedral iron ore, red mud or their mixture.
22. according to above-mentioned 18 submethod, the consumption of wherein said (I) class catalyzer is 5-15wt%, the wt% dry weight based on carbon-contained organic matter.
23. according to above-mentioned 18 submethod, the consumption of wherein said (II) class catalyzer is 2-10wt%, the wt% dry weight based on carbon-contained organic matter.
24. according to above-mentioned 18 submethod, the consumption of wherein said (III) class catalyzer is 20-30wt%, the wt% dry weight based on carbon-contained organic matter.
25. according to the above-mentioned submethod of 1,4,7 or 10, and wherein said high-pressure water heating refers to the water of temperature 300-374 DEG C and more than pressure 22MPa.
26. according to according to the above-mentioned submethod of 1,4,7 or 10, and wherein said high-pressure water heating refers to the water of temperature more than 374 DEG C and pressure 3-22MPa.
27. according to the above-mentioned submethod of 1,4,7 or 10, and wherein said supercritical state is that temperature and pressure is respectively more than 374 DEG C with the water of 22MPa.
28. according to the above-mentioned submethod of 1,4,7 or 10, and wherein the residence time of reactant in reactor is 15-200 second.
29. according to the above-mentioned submethod of 1,4,7 or 10, and wherein the residence time of reactant in reactor is 16-30 second.
30. according to the above-mentioned submethod of 3,6,9 or 12, and wherein said reducing valve is needle type valve.
31. high-pressure water heatings/supercritical water gasification subsystem, comprise reactor (4), the first separator (6), the second separator (7), it is characterized in that between described reactor (4) and the first separator (6) and/or between described first separator (6) and the second separator (7), be provided with the equipment can discharged for material decompressing and continuous.
32. according to above-mentioned 31 subsystem, wherein said for material decompressing and continuous discharge equipment comprise at least two surge tanks be connected in parallel to each other.
33. according to above-mentioned 31 subsystem, wherein said for material decompressing and continuous discharge equipment comprise at least one needle type valve.
34. according to above-mentioned 31 subsystem, wherein said device also comprises preheater (3) to be preheated to temperature required by described slurry with high temperature rise rate.
35. according to above-mentioned 34 subsystem, wherein said preheater (3) is selected from Hi-frequency electromagnetic heater or microwave heater or gas combustion heaters.
Carbon-contained organic matter alleged in the present invention includes but not limited to:
Coal, comprises the coal of all kinds, and such as hard coal, bituminous coal, brown coal, mud coal, algal coal etc., also comprise the semicoke produced by coal, tar, wax, the coal-based product such as pitch;
Oil, comprises the boat coal produced in various oil and petroleum refining process, gasoline, kerosene, diesel oil, the petroleum-based products such as wax, tar, pitch;
Biomass, comprise grain, stalk, vegetables, algae etc.;
Other organic substance, comprises damaged tire, the organic waste matter such as plastic waste, and organic domestic waste;
Or described carbonaceous material can also comprise the mixture of above-named each material.
Embodiment of the present invention are illustrated below in conjunction with Fig. 1 and Fig. 2.
In fig. 1 and 2, before step of the present invention a), use conventional means that carbon-contained organic matter is ground into powder, the granularity of powder is less than 0.3mm, preferred 0.05mm-0.2mm.Then this powder and water are mixed and made into the slurry that powder concentration is 10-60wt%, preferably 50-60wt%, wherein wt% is based on the gross weight of slurry.Slurry is placed in slurry can 1.Optionally, catalyzer can be added in slurry, or catalyzer also can not to join in slurry but to join separately in reactor.Catalyzer of the present invention can be selected from following a few class: (I) basic metal or alkaline earth metal oxide, basic metal or alkaline earth salt or basic metal or alkaline earth metal hydroxides or their mixture; (II) one or more transition metal on carrier are carried on; (III) mineral substance of iron content.Such as, (I) class catalyzer can be K
2o, Na
2o, CaO, MgO, NaOH, KOH, Ca (OH)
2, Mg (OH)
2, K
2cO
3, Na
2cO
3or their mixture; (II) class catalyzer can be the composite catalyst such as Ni, Ru, the Fe be carried on carrier or K-Ni, K-Fe, the K-Ni-Fe be carried on carrier; (III) class catalyzer can be Fe
3o
4, peridotites, rhombspar, rhombohedral iron ore, red mud or their mixture.Catalyzer also can be the mixture of above-mentioned all kinds of catalyzer.If use (I) class catalyzer, its consumption is the 5-15wt% of powder weight.If use (II) class catalyzer, its consumption is the 2-10wt% of powder weight.If use (III) class catalyzer, its consumption is the 10-30wt% of powder weight.
By high-pressure pump 2, above-mentioned slurry is forced into the pressure wanted, such as close to or reach the pressure of high-pressure water heating defined herein or the pressure of the supercritical state of water.
Before step of the present invention a), optionally can also comprise and be preheated to temperature required step to described slurry with high temperature rise rate, this step is carried out in preheater 3.The benefit adopting high temperature rise rate to heat material one can be made to enter reactor 4 can react, effectively shorten its residence time in reactor, such as, in certain embodiments, the residence time of material in reactor can be 0.5-10 minute, preferred 2-5 minute, thus the generation decreasing the macromolecular substance such as the tar causing blocking, reduce the risk of logistics sedimentation or coking and blocking in reactor.Described high temperature rise rate is 30-50 DEG C/min.Temperature rise rate high like this can realize by increasing preheater power, and such as, by high-frequency electromagnetic heating or microwave heating or realized by gaseous combustion, the mode also accompanying by self-heating by logical oxygen combustion has been come.
Supercritical state in the present invention and high-pressure water heating state are that the temperature and pressure of water is for the state of the stagnation point of water, the supercritical state of water refer to temperature and pressure respectively more than 374 DEG C and 22MPa time water, high-pressure water heating refers to that temperature is at 300 ~ 374 DEG C, pressure more than the water of 22MPa or temperature more than 374 DEG C, the water of pressure between 3-22MPa.
Described high concentration slurry reacts with the water of high-pressure water heating or supercritical state under the effect of catalyzer, forming reactions product.This reaction product optionally tentatively cools in interchanger 5 in reactor 4 exit, to reclaim a part of heat.
Then, in the embodiment depicted in fig. 1, described reaction product decompressing and continuous is discharged in the first separator 6.Described " decompressing and continuous discharge " is realized by least two surge tanks be connected in parallel to each other 8 between reactor 4 and the first separator 6, wherein under continuous duty, have at least a surge tank to be used for receiving the reaction product of autoreactor 4, and have a surge tank at least for received reaction product is discharged to the first separator 6.Above-mentioned surge tank not only plays liquid storage effect, also plays the effect of reducing pressure to the reaction product of High Temperature High Pressure simultaneously.After the surge tank for splicing is full of, then switched to discharge state to the first separator 6 discharge; And after the surge tank of discharge is emptying, then being switched tieback material state, the surge tank of multiple parallel connection, with this semi-batch mode alternate run, ensure that the continuous operation of its step upstream and downstream procedures.
Or as alternate embodiment, as shown in Figure 2, described " decompressing and continuous discharge " also can be realized by least one reducing valve 9 between reactor 4 and the first separator 6, described valve such as needle type valve.Reaction product is discharged continuously after reducing valve decompression again.Such reducing valve has one at least, but considers from reliability perspectives, and such reducing valve preferably has multiple, and multiple reducing valve can serial or parallel connection.In order to protect reducing valve, a ball valve 11 optionally can also be added to protect reducing valve before reducing valve.
In the first separator 6, carry out product separation through the reaction product that decompression is discharged continuously, obtain gaseous product and liquid-solid mixture, wherein gaseous product comprises inflammable gas, such as hydrogen, methane, carbon monoxide etc.Described first separator can be the gas/liquid separation of this area routine, such as cyclonic separator, baffle separation or filler separation.Gu be discharged to by liquid-solid mixture in the second separator 7 and carry out liquid/separation, obtain product liquid and solid product.This second separator can be liquid/solid separator well known to those skilled in the art, such as centrifuge separator or settlement separator.
When use (I) class catalyzer, solid product after separation is reacted residue, and the product liquid after being separated obtains oil phase and aqueous phase again after layering, oil phase is tar mainly, it can be processed further and be separated obtained various oil product, or optionally turns back in slurry and reenter in reactor.And aqueous phase, it comprises (I) class catalyzer of solubility, then can again be used for preparing slurry.When use (II) and (III) class catalyzer, because it is water insoluble, catalyzer discharges the second separator as a part for solid residue, optionally reclaims catalyzer from from this solid residue.
Below by reference to the accompanying drawings embodiment of the present invention are described, but it will be understood by those skilled in the art that, obviously can also change above-mentioned embodiment and not deviate from purport of the present invention, such as, the described surge tank for " decompressing and continuous discharge " or reducing valve also can not between reactors 4 and the first separator 6, but be between the first separator 6 and the second separator 7, as shown in Figure 3; Or, described surge tank or reducing valve can be set between reactor 4 and the first separator 6 and between the first separator 6 and the second separator 7 to realize " decompressing and continuous discharge ".Or described surge tank and reducing valve can combinationally use.Or, also the first separator 6 and the second separator 7 can be merged into a gas-liquid-solid three-phase separator 10, as shown in Figure 4.
On the other hand, present invention provides high-pressure water heating/supercritical water gasification subsystem, comprise reactor 4, first separator 6, second separator 7, it is characterized in that between described reactor 4 and the first separator 6 and/or between the first separator 6 and the second separator 7, be provided with the equipment can discharged for material decompressing and continuous.As mentioned above, this equipment can discharged for material decompressing and continuous can comprise at least two surge tanks be connected in parallel to each other, or this equipment can discharged for material decompressing and continuous can be at least one reducing valve such as needle type valve, described reducing valve can in parallel or series connection.
In subsystem as above, also optionally comprise preheater 3 such as Hi-frequency electromagnetic heater or microwave heater or gas combustion heaters to be preheated to temperature required by described slurry with high temperature rise rate.
Integrated approach of the present invention, except comprising high-pressure water heating/supercritical water gasification submethod, also can comprise Poly-generation submethod, method that algae inhales carbon submethod and/or compound energy hydrogen manufacturing submethod and/or recover materials and energy.
Two. Poly-generation submethod and subsystem
Poly-generation submethod be used for high-pressure water heating of the present invention/supercritical water gasification submethod to produce gas delivery go out the synthetic gas after methane and utilize further with at least one in methanol, methane, ethylene glycol, low-carbon alcohol, dme.Poly-generation submethod can allocate appropriate hydrogen or supplementary carbon monoxide into regulate hydrogen-carbon ratio.Synthetic gas is utilized to produce the method for these products and device is all known in this area.
Three. algae inhales carbon submethod and subsystem
In order to realize carbonic acid gas close to zero release, integrated approach of the present invention also comprises algae and inhales carbon submethod in order to absorb the final remaining carbonic acid gas of described integrated approach.
Described algae inhales carbon technique, is utilize the photosynthesis of algae to absorb the carbonic acid gas produced in integrated approach of the present invention, produces oxygen and biomass simultaneously.Described biomass can be used to production biofuel, also can be used to produce the high value added products such as astaxanthin, carotenoid, phycobiliprotein, the algae residue produced can directly process as fertilizer etc., also can be passed through one or more in biological fermentation generation methane, hydrogen or ethanol.Algae residue after fermentation can return high-pressure water heating/supercritical water gasification subsystem and coal is mixed with carbon-contained organic matter.The hydrogen produced can return high-pressure water heating/supercritical water gasification submethod and Poly-generation submethod, forms circulation technology.The oxygen capable of circulation time high-pressure water heating/supercritical water gasification submethod produced.
Algae inhales carbon can adopt the common algae such as Euglena, green alga, stonewort, chrysophyceae, dinoflagellate, red algae, diatom, chlamydomonas, xanthophyta, brown alga or blue-green algae.
In system, isolated carbon dioxide, removes solid particulate after filtration, and be collected into by air pump lead-in light bio-reactor after gas reservoir, the breather be connected with bioreactor can choose nozzle-type, aeration hair style or other all kinds.Under certain temperature range (10 ~ 40 DEG C), intensity of illumination (300 ~ 40000LUX), the Euglena absorbing carbon dioxide cultivated in bioreactor, carry out photosynthesis, under visible light illumination, be glucose by carbon dioxide transitions, and then be converted into the nutritive substances such as protein, fat, VITAMIN, discharge a large amount of oxygen simultaneously.Euglena is converted into biomass through cultivation, one or more in biological refinement technique production biofuel, astaxanthin, carotenoid, phycobiliprotein of biomass.
Four, compound energy hydrogen manufacturing submethod and subsystem
Integrated approach of the present invention also comprises compound energy hydrogen manufacturing submethod to provide hydrogen and/or the oxygen of method needs of the present invention.
Compound energy hydrogen manufacturing submethod is selected from Water electrolysis hydrogen production method, biological hydrogen production method, bioelectrochemistry hydrogen production process or PhotoelectrochemicalSystem System for Hydrogen Production method.The energy needed for compound energy hydrogen manufacturing submethod is from sun power, wind energy, water energy, Geothermal energy, tidal energy, nuclear power, valley electricity, thermoelectricity equal energy source.
Described Water electrolysis hydrogen production method, its water electrolysis mode can adopt solid polymer electrolyte (Solid Polymer Electrolyte, SPE) electrolyzer system, also can adopt traditional alkaline electrolysis tank systems, can also adopt solid polymer electrolyte electrolytic bath system.
Wherein, the water electrolysis system based on solid polymer electrolyte can be divided into two parts on the whole: process portion and circuit control part, for reducing the application of explosion-proof component, two portions can be separated and seal.Process portion generally comprises electrolytic module, water supply module and gas cleaning module, for ensureing the safety of electrolytic process, generally can add gas alarm equipment in this part and purge facility; Circuit control part generally comprises supply module, electrical instrument control module and multi-pole switch module, for simplifying this part, circuit generally can be adopted integrated and controlled by remote computer.Water electrolysis system (SPE-WE) technology of solid polymer electrolyte can direct production high-purity (> 99.9999%) and high pressure (> 10MPa) hydrogen, volume is little, hydrogen output is high, and can work in coordination with renewable energy system and fuel cell system the green circulatory forming the energy.
Alkaline electrolytic bath mainly contains two kinds: traditional alkaline electrolytic bath (AlkalineElectrolyzer) and emerging solid polymer electrolytic groove.The seventies in last century rises, and investigator turns to alkaline polymer electrolyte (Alkaline Solid PolymerElectrolyte, ASPE) sight.What ASPE conducted is hydroxide ion, instead of proton, and Working environment becomes alkalescence by acidity, both as the barrier film of isolating hydrogen and oxygen, is played again the effect of conduction by conduction hydroxide ion.ASPE alkaline electrolytic bath uses base metal as catalyzer, and at present based on nickel-base catalyst, other non-precious metal catalysts are auxiliary binary or multicomponent catalyst.In alkaline electrolytic bath, catalyzer is electroplated in bipolar plates by electrochemical method.Therefore, catalyzer and bipolar plates are integral types.In bipolar plates, alkaline electrolytic bath uses bipolar plate of stainless steel, and its effect not only makees pole plate but also work as catalyst substrate.In alkaline system, stainless steel also possesses chemical stability.Compared with conventional alkaline electrolyzer, novel alkaline polymer electrolyte membrane is nontoxic, pollution-free, and its mechanical property, stability and cost all have good advantage.Replace poisonous asbestos diaphragm, electrolytic solution has been replaced with deionized water by the potassium hydroxide solution of 25-30wt% concentration, avoids the erosion of alkali lye, effectively increases the work-ing life of electrolyzer, reduces maintenance cost.In current density, the relative alkaline electrolytic bath of current efficiency is improved.In electrode preparation, ASPE, as solid polymer dielectric film, needs to prepare membrane electrode, adopt stainless steel flow field as pole plate, and alkaline electrolytic bath is generally electroplated Ni base non-precious metal catalyst on stainless steel polar plate simultaneously.
Described biological hydrogen production method, includes but not limited to take biomass as the prepared using ermal physics principles of chemistry and technology hydrogen making and utilize bio-metabolic process that organism or water are converted into hydrogen.The latter includes but not limited to photosynthetic organism direct hydrogen production and biomass ferment hydrogen manufacturing.
The microbe species of biological hydrogen production comprises photosynthetic organism (anaerobism photosynthetic bacterium, cyanobacteria and green alga), non-photosynthetic organism (strict anaerobe, facultative anaerobic bacteria and aerobic bacteria) and archeobacteria monoid.Photosynthetic conversion solar wherein in cyanobacteria and green algae bioavailable body can be Hydrogen Energy.Photodestruciton aquatic products hydrogen is desirable hydrogen manufacturing approach, but puts hydrogen simultaneously photosynthetic, with the release of oxygen, except hydrogen generation efficiency is lower, also along with the key issue of putting hydrogen enzyme chance oxygen inactivation; The anaerobism of anaerobism photosynthetic bacterium is photosynthetic puts hydrogen process non-oxygen-production, and technique is simple, produce hydrogen purity and hydrogen generation efficiency high; Non-photosynthetic organism degradable larger molecular organics produces the characteristic of hydrogen, makes it in bio-transformation renewable energy source material (Mierocrystalline cellulose and degraded product and starch etc.) production Hydrogen Energy.
Biological hydrogen production process can fall into 5 types: (1) utilizes the biophotolysis water law of algae or ultramarine bacterium; (2) the photosynthetic bacteria used for light decomposition method of organic compound; (3) ferment for hydrogen production of organic compound; (4) the coupled method hydrogen manufacturing of photosynthetic bacterium and fermenting bacteria; (5) enzyme catalysis method hydrogen manufacturing.The hydrogen-producing speed of current fermenting bacteria is higher, and lower to conditional request, has direct application prospect.
Described bioelectrochemistry hydrogen production process, be by microbiological fuel cell (MFC) technical development, MFC is based on the anaerobic respiration based on microorganism, is namely the electron transfer process of sole electron acceptor with negative electrode.In MFC working process, first some microbiological oxidation organic substrates produce electronics and proton, transfer transport is to anode, negative electrode is delivered to by wire after being accepted by anode, proton penetrates into cathode compartment by cationic exchange membrane from anolyte compartment, negative electrode generates water with oxygen and electronic action, by electron flow generation current continuously.Bioelectrochemistry hydrogen system, the running near anode is similar to MFC, and bacterial oxidation organism generates carbonic acid gas, proton and electronics, and electronics is transferred to anode, and prototropy is to negative electrode.The running of negative electrode and MFC distinguish larger, cathode reaction chambers is airtight, keeps oxygen-free environment, utilizes external power in MFC circuit, strengthen the electromotive force of negative electrode by electrochemical method, energy needed for part bacterial growth is provided on the one hand, provides electronics to negative electrode on the other hand.And be directly used as electron acceptor(EA) at negative electrode proton, produce hydrogen.This method utilizes organism direct production hydrogen, significantly reduces energy consumption compared with brine electrolysis.The method utilizes the voltage being greater than 110mV (as 300mV ~ 400mV), and theoretical cathode just can produce hydrogen.The voltage (theoretical 1210mV, electrolytic solution pH are for neutral) that this voltage produces hydrogen than brine electrolysis is low many.Adopt bioelectrochemistry hydrogen producing technology can be then matrix product hydrogen with the tunning after biological hydrogen production, organic waste water etc.Using acetic acid as matrix, impressed voltage is 250mV is example, produces 1m
3hydrogen only needs the electricity of 0.6kWh, and brine electrolysis produces 1m
3hydrogen then needs to consume electricity 4.5 ~ 5kWh.
Described PhotoelectrochemicalSystem System for Hydrogen Production method is a kind of low cost hydrogen producing technology converting solar energy into Hydrogen Energy.Be converted in the process of Hydrogen Energy at sun power, utilize photoelectric-synergetic effect to reach the object improving phototransformation rate.In PhotoelectrochemicalSystem System for Hydrogen Production system, conductor photocatalysis material is as light anode, electron-hole pair is produced after light anode absorb photons, hole has stronger oxidation capacity, hydroxide ion in water is oxidized to oxygen, electronics has stronger reducing power, is transferred to proton in cathodic reduction water and generates hydrogen under applying bias effect.
Five, the submethod of recover materials and energy and subsystem
Method of the present invention also comprises catalyzer, water or the steam reclaimed in described method, solid materials circulate it, and utilizes the waste heat in described method or top pressure power generation or produce steam.This clearly demarcated integrated approach is further illustrated below in conjunction with accompanying drawing 5-7.
See Fig. 5, the exit gas of the first separator 6 (mainly contains CH
4, CO, H
2and CO
2) be isolated to methane, residue H
2poly-generation subsystem 12 is sent into for the preparation of methane, methyl alcohol, dme etc. with CO.The steam that Poly-generation submethod produces sends into generator 13 for generating.
See Fig. 6, the synthetic gas of gas after separation of methane (the mainly H that high-pressure water heating/supercritical water gasification subsystem is produced
2and CO) and the hydrogen produced of hydrogen manufacturing subsystem and algae inhale the byproduct hydrogen mixing that algae residue that carbon subsystem produces produces through fermentation, send into Poly-generation subsystem, part direct methanation prepares methane, and water byproduct can return high-pressure water heating/supercritical water gasification subsystem.Another part synthesizing methanol, a part for the methyl alcohol of production is for the production of dme, and another part can direct marketing.The carbonic acid gas that high-pressure water heating/supercritical water gasification subsystem and Poly-generation subsystem generate is sent into algae and is inhaled carbon subsystem production biofuel, the oxygen of coproduction simultaneously.Algae residue returns Poly-generation subsystem for one or more in fermentative production byproduct hydrogen, methane or ethanol, byproduct hydrogen.Algae residue after fermentation returns high-pressure water heating/supercritical water gasification subsystem and coal is mixed with carbon-contained organic matter.The waste water produced in algae residue and system also can be used for bioelectrochemistry hydrogen manufacturing.The energy needed for hydrogen manufacturing subsystem is from compound energies such as sun power, wind energy, water energy, Geothermal energy, tidal energy, nuclear power, valley electricity, thermoelectricitys.Hydrogen manufacturing subsystem is as adopted water electrolysis hydrogen production, and the oxygen of generation and algae inhale the oxygen mix that carbon subsystem produces, and sends into high-pressure water heating/supercritical water gasification subsystem.
See Fig. 7, rough coal first carries out Coal pretreatment under subcritical or supercritical state, and from coal dust, removing also obtains the materials such as montanin wax, anthracene, phenanthrene, naphthalene through tripping device deep processing.The coal dust surface super cleaning and porous of this process, its character is similar to gac or skeleton carbon, and the high concentration slurry that the algae residue after then making the coal dust of this process and fermenting, catalyst mix prepare carbon-contained organic matter enters high-pressure water heating/supercritical water gasification subsystem.Wherein said subcritical state is 16-22MPa and 120-374 DEG C.
The byproduct hydrogen mixing that the algae residue that the hydrogen that hydrogen manufacturing subsystem produces and algae inhale the generation of carbon subsystem produces through biological fermentation, a part returns high-pressure water heating/supercritical water gasification subsystem for mending hydrogen, and another part sends into Poly-generation subsystem.The synthetic gas of gas after separation of methane (the mainly H that high-pressure water heating/supercritical water gasification subsystem is produced
2and CO) send into Poly-generation subsystem, a part of direct methanation prepares methane, and water byproduct returns high-pressure water heating/supercritical water gasification subsystem; Another part synthesizing methanol, a part for the methyl alcohol of production is for the production of dme, and another part can direct marketing.The carbonic acid gas that high-pressure water heating/supercritical water gasification subsystem and Poly-generation subsystem generate is sent into algae and is inhaled carbon subsystem production biofuel, the oxygen of coproduction simultaneously.Algae residue produces one or more in byproduct hydrogen, methane or ethanol for biological fermentation; Byproduct hydrogen returns Poly-generation subsystem.Algae residue after fermentation returns the high concentration slurry that high-pressure water heating/supercritical water gasification subsystem and coal are mixed with carbon-contained organic matter, sends into high-pressure water heating/supercritical water gasification reactor.The waste water produced in algae residue and system also can be used for bioelectrochemistry hydrogen manufacturing.The energy needed for hydrogen manufacturing subsystem is from compound energies such as sun power, wind energy, water energy, Geothermal energy, tidal energy, nuclear power, valley electricity, thermoelectricitys.Hydrogen manufacturing submethod is as adopted water electrolysis hydrogen production, and the oxygen of generation and algae inhale the oxygen mix that carbon subsystem produces, and sends into high-pressure water heating/supercritical water gasification subsystem.
Embodiment
Embodiment 1
Get the dry pulverized coal that granularity is less than 75 μm, be configured to the slurry of 10 ~ 30wt%, then add the potassium carbonate catalyst of dry coal massfraction 10%, stir;
Open high-pressure pump 2 first to suppress whole device with water, until the pressure in reactor rises to 25MPa or 30MPa, change into and pump into slurry, after system pressure is stable, open reactor heating power supply, setting reactor center temperature is 650 DEG C or 550 DEG C, and the preheating temperature of setting coal water slurry is up to 300 DEG C.The rapid reaction in reactor of slurry after preheating, 30 seconds-1 minute residence time.Reaction product enters one in surge tank 8 after water cooler 5 is cooled to 80 DEG C, after this surge tank is full of, be switched to another surge tank, then pressure release is carried out to the surge tank be full of, reaction product after pressure release enters the first separator 6 and carries out gas/liquid and be admittedly separated, be separated the gas obtained to discharge from this separator top, Gu the liquid-solid mixture that separation obtains enters the second separator 7 carry out liquid/separation.Actual conditions and the result of this embodiment are shown in table 1.
Table 1
Embodiment 2
Sunflower Receptacle stalk is milled to below 80 orders with micro-algae residue, is made into water the slurry that concentration is 20wt%, adds slurry can 1, then add the K-N i composite catalyst be carried on carrier of dry powder quality mark 5%, stir.
Open high-pressure pump 2 first to suppress system with water, until system pressure rises to 25MPa, change into and pump into slurry, after system pressure is stable, open reactor 4 heating power supply, setting reactor center temperature is 350 DEG C or 400 DEG C, and setting slurry preheating temperature is up to 200 DEG C.The rapid reaction in reactor of slurry after preheating, residence time 1-10 minute.Reaction product enters the first separator 6 and carries out gas/liquid and be admittedly separated after water cooler 5 is cooled to 80 DEG C, the gaseous product obtained is discharged from separator top drilling, safety valve can be set on this gas tube as required, gaseous tension is dropped to required pressure, the liquid-solid mixture obtained then decompressing and continuous is discharged to one of surge tank 8, after this surge tank is full of, switch to another surge tank, then pressure release is carried out to the surge tank 7 be full of, Gu make liquid-solid mixture enter the second separator 7 carry out liquid/separation.Actual conditions and the result of this embodiment are shown in table 2.
Table 2
Embodiment 3
Crude oil is made into through the irreducible oil of underpressure distillation gained the slurry that concentration is 30-40wt% together with water, tensio-active agent, adds slurry can 1, then add relative to residua weight 15% the K-Ni composite catalyst be carried on carrier, stir.
Open high-pressure pump 2 first to suppress system with water, until system pressure rises to 28MPa, change into and pump into slurry, after system pressure is stable, open reactor 4 heating power supply, setting reactor center temperature is 600 DEG C, and setting slurry preheating temperature is up to 200 DEG C.The rapid reaction in reactor of slurry after preheating, 2 minutes residence time.Reaction product enters the first separator 6 and carries out gas/liquid and be admittedly separated after water cooler 5 is cooled to 80 DEG C, the gaseous product obtained is discharged from separator top drilling, safety valve can be set on this gas tube as required, gaseous tension is dropped to required pressure, Gu the liquid-solid mixture obtained then is discharged to the second separator 7 through needle type valve decompressing and continuous carry out liquid/separation.Actual conditions and the result of this embodiment are shown in table 3.
Table 3
Advantage of the present invention is as follows:
1. according to different material characteristics and products scheme, take high-pressure water heating or supercritical water reaction respectively, and add different catalyzer, technological process is flexible.
2. high heating rate, contributes to improving material flow, reduces reaction time, the macromole such as polyreaction, tar effectively can be suppressed to generate, suppress coking, be conducive to alleviating latch up phenomenon.
3. a plurality of fluids is with different angles charging, ensure that the mixed effect of material.
4. surge tank can not only play liquid storage effect, can also play depressurization, be separated after decompression to fluid again, reduce equipment requirements, operates more safe and reliable.
In addition can adjust separator and surge tank position according to actual needs, select the separation of corresponding high pressure or low pressure to be separated or high-low pressure separation and combination.
5. the continuous discharge of liquid-solid fluid especially solid residue ensure that the continuity of system cloud gray model.
6. the near zero release of carbonic acid gas.On the one hand inhale carbon technique by algae, catch, absorbing carbon dioxide, on the other hand by joining Hydrochemistry carbon-fixation-technology, carbon monoxide or carbonic acid gas all being changed into energy product, thus realize carbonic acid gas near zero release.
7. the full price exploitation of coal resources and the optimum use of resource.Coal is converted into methane, hydrogen, methyl alcohol, ethylene glycol, low-carbon alcohol and/or dme; By compound energy hydrogen producing technology, save Kong Fen workshop section; Utilize biological refinement technique to obtain biofuel, the level of resources utilization can reach more than 80%.
Claims (33)
1. utilize an integrated approach for carbon-contained organic matter, comprise
High-pressure water heating/supercritical water gasification submethod and Poly-generation submethod, wherein said high-pressure water heating/supercritical water gasification submethod comprises:
A) in reactor (4), the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product, wherein said high-pressure water heating refer to temperature be 300 ~ 374 DEG C and pressure more than the water of 22MPa or temperature more than 374 DEG C and the water of pressure between 3-22MPa;
B) described reaction product decompressing and continuous is discharged in the first separator (6);
C) make reaction product carry out gas/liquid in the first separator (6) to be admittedly separated, obtain gaseous product and liquid-solid mixture, wherein gaseous product comprises inflammable gas, discharges this gaseous product; Liquid-solid mixture is then discharged in the second separator (7);
D) at the second separator (7) Gu in liquid/separation is carried out to liquid-solid mixture, obtain product liquid and solid residue, and discharge respectively continuously;
Wherein carry out implementation step b by least two surge tanks be connected in parallel to each other (8) be positioned between reactor (4) and the first separator (6)), wherein under continuous duty, have at least a surge tank to be used for reception and carry out the reaction product of autoreactor (4), and have a surge tank at least for the reaction product received being discharged in the first separator (6).
2. integrated approach according to claim 1, wherein carrys out implementation step b by least one reducing valve (9) be positioned between reactor (4) and the first separator (6)).
3. integrated approach according to claim 1, wherein said Poly-generation submethod utilizes at least one in described high-pressure water heating/isolated producing firedamp by syngas of supercritical water gasification submethod, low-carbon alcohol, dme.
4. utilize an integrated approach for carbon-contained organic matter, comprise
High-pressure water heating/supercritical water gasification submethod and Poly-generation submethod, wherein said high-pressure water heating/supercritical water gasification submethod, comprising:
A) in reactor (4), the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product, wherein said high-pressure water heating refer to temperature be 300 ~ 374 DEG C and pressure more than the water of 22MPa or temperature more than 374 DEG C and the water of pressure between 3-22MPa;
B) make reaction product be discharged to the first separator (6) continuously, and in the first separator (6), carry out gas/liquid be admittedly separated, obtain gaseous product and liquid-solid mixture, wherein gaseous product comprises inflammable gas, discharges this gaseous product;
C) by step b) liquid-solid mixture decompressing and continuous be discharged in the second separator (7);
D) at the second separator (7) Gu in liquid/separation is carried out to described liquid-solid mixture, obtain product liquid and solid residue, and discharge respectively continuously;
Wherein carry out implementation step c by least two surge tanks be connected in parallel to each other (8) be positioned between the first separator (6) and the second separator (7)), wherein under continuous duty, have at least a surge tank to be used for receiving the liquid-solid mixture from the first separator (6), and have a surge tank at least for liquid-solid mixture being discharged to the second separator (7).
5. integrated approach according to claim 4, wherein carrys out implementation step c by least one reducing valve be positioned between the first separator (6) and the second separator (7)).
6. integrated approach according to claim 4, wherein said Poly-generation submethod utilizes at least one in described high-pressure water heating/isolated producing firedamp by syngas of supercritical water gasification submethod, low-carbon alcohol, dme.
7. utilize an integrated approach for carbon-contained organic matter, comprise
High-pressure water heating/supercritical water gasification submethod and Poly-generation submethod, wherein said high-pressure water heating/supercritical water gasification submethod, comprising:
A) in reactor (4), the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product, wherein said high-pressure water heating refer to temperature be 300 ~ 374 DEG C and pressure more than the water of 22MPa or temperature more than 374 DEG C and the water of pressure between 3-22MPa;
B) described reaction product decompressing and continuous is discharged in the first separator (6);
C) make reaction product carry out gas/liquid in the first separator (6) to be admittedly separated, obtain gaseous product and liquid-solid mixture, wherein gaseous product comprises inflammable gas, discharges this gaseous product;
D) by step c) liquid-solid mixture decompressing and continuous be discharged in the second separator (7);
E) at the second separator (7) Gu in liquid/separation is carried out to described liquid-solid mixture, obtain product liquid and solid residue, and discharge respectively continuously;
Wherein carry out implementation step b by least two surge tanks be connected in parallel to each other (8) be positioned between reactor (4) and the first separator (6)), wherein under continuous duty, have at least a surge tank to be used for reception and carry out the reaction product of autoreactor (4), and have a surge tank at least for the reaction product received being discharged in the first separator (6); And carry out implementation step d by least two surge tanks be connected in parallel to each other be positioned between the first separator (6) and the second separator (7)), wherein under continuous duty, have at least a surge tank to be used for receiving the liquid-solid mixture from the first separator (6), and have a surge tank at least for liquid-solid mixture being discharged to the second separator (7).
8. integrated approach according to claim 7, wherein carry out implementation step b by least one reducing valve be positioned between reactor (4) and the first separator (6)), and wherein carry out implementation step d by least one reducing valve be positioned between the first separator (6) and the second separator (7)).
9. integrated approach according to claim 7, wherein said Poly-generation submethod utilizes at least one in described high-pressure water heating/isolated producing firedamp by syngas of supercritical water gasification submethod, low-carbon alcohol, dme.
10. utilize an integrated approach for carbon-contained organic matter, comprise
High-pressure water heating/supercritical water gasification submethod and Poly-generation submethod, wherein said high-pressure water heating/supercritical water gasification submethod, comprising:
A) in reactor (4), the high concentration slurry of carbon-contained organic matter is made to react under high-pressure water heating or supercritical water state in the presence of a catalyst, forming reactions product, wherein said high-pressure water heating refer to temperature be 300 ~ 374 DEG C and pressure more than the water of 22MPa or temperature more than 374 DEG C and the water of pressure between 3-22MPa;
B) described reaction product decompressing and continuous is discharged in gas-liquid-solid three-phase separator (10);
C) make reaction product at gas-liquid-solid three-phase separator (10) Gu in carry out gas/liquid/separation, obtain gaseous product, product liquid and solid product, wherein gaseous product comprises inflammable gas, respectively continuous Exhaust Gas product, product liquid and solid product;
Wherein realize step b by least two surge tanks be connected in parallel to each other be positioned between reactor (4) and gas-liquid-solid three-phase separator (10)), wherein under continuous duty, have at least a surge tank to be used for reception and carry out the reaction product of autoreactor (4), and have a surge tank at least for the reaction product received being discharged in gas-liquid-solid three-phase separator (10).
11. integrated approachs according to claim 10, wherein realize step b by least one reducing valve (9) be positioned between reactor (4) and gas-liquid-solid three-phase separator (10)).
12. integrated approachs according to claim 10, wherein said Poly-generation submethod utilizes at least one in described high-pressure water heating/isolated producing firedamp by syngas of supercritical water gasification submethod, low-carbon alcohol, dme.
13. integrated approachs according to claim 12, also comprise algae and inhale carbon submethod.
14. integrated approachs according to claim 13, wherein said algae inhales carbon submethod and absorbs the final remaining carbonic acid gas of described integrated approach with at least one in production biofuel, oxygen, hydrogen, methane, ethanol, astaxanthin, carotene, phycobiliprotein.
15. according to the integrated approach of claim 13 or 14, and wherein said algae inhales carbon submethod and uses Euglena, green alga, stonewort, chrysophyceae, dinoflagellate, red algae, diatom, chlamydomonas, xanthophyta, brown alga or blue-green algae.
16. integrated approachs according to claim 15, are mixed with the high concentration slurry of described carbon-contained organic matter with coal, feeding reactor (4) after the residue fermentation of described algae.
17. integrated approachs according to claim 12, also comprise compound energy hydrogen manufacturing submethod.
18. integrated approachs according to claim 17, wherein compound energy hydrogen manufacturing submethod is selected from Water electrolysis hydrogen production method, biological hydrogen production method, bioelectrochemistry hydrogen production process or PhotoelectrochemicalSystem System for Hydrogen Production method.
19. integrated approachs according to claim 12, also comprise catalyzer, water or the steam reclaimed in described integrated approach, solid materials circulate it, and utilize the waste heat in described integrated approach or top pressure power generation or produce steam.
20. methods according to claim 17, the electric energy that energy required in wherein said compound energy hydrogen manufacturing submethod is selected from sun power, wind energy, water energy, Geothermal energy, tidal energy, nuclear power, valley electricity, thermoelectricity or produces according to claim 16.
21. integrated approachs according to claim 13, also comprise compound energy hydrogen manufacturing submethod.
22. methods according to claim 18, energy required in wherein said compound energy hydrogen manufacturing submethod is selected from sun power, wind energy, water energy, Geothermal energy, tidal energy, nuclear power, valley electricity or thermoelectricity.
23. integrated approachs as claimed in claim 12, wherein said Poly-generation submethod utilizes at least one in the isolated synthetic gas methanol of described high-pressure water heating/supercritical water gasification submethod, ethylene glycol.
24. 1 kinds of system ensembles utilizing carbon-contained organic matter, comprise high-pressure water heating/supercritical water gasification subsystem and Poly-generation subsystem, wherein said high-pressure water heating/supercritical water gasification subsystem comprises reactor (4), the first separator (6), the second separator (7), it is characterized in that between described reactor (4) and the first separator (6) and/or between described first separator (6) and the second separator (7), be provided with the equipment can discharged for material decompressing and continuous; Wherein said high-pressure water heating refer to temperature be 300 ~ 374 DEG C and pressure more than the water of 22MPa or temperature more than 374 DEG C and the water of pressure between 3-22MPa;
The wherein said equipment for the discharge of material decompressing and continuous comprises at least two surge tanks be connected in parallel to each other.
25. system ensembles according to claim 24, the wherein said equipment for the discharge of material decompressing and continuous comprises at least one needle type valve.
26. system ensembles according to claim 24, wherein said device also comprises preheater (3) to be preheated to temperature required by described slurry with high temperature rise rate.
27. system ensembles according to claim 26, wherein said preheater (3) is selected from Hi-frequency electromagnetic heater or microwave heater or gas combustion heaters.
28. according to the system ensemble of any one of claim 24-26, and wherein said Poly-generation subsystem produces at least one in methane, low-carbon alcohol, dme.
29. system ensembles according to claim 28, also comprise algae and inhale carbon subsystem, described algae inhales carbon subsystem and absorbs the remaining carbonic acid gas of described system ensemble.
30. system ensembles according to claim 28, also comprise compound energy hydrogen manufacturing subsystem, and described compound energy hydrogen manufacturing subsystem is selected from hydrogen production plant by water electrolysis, biological hydrogen production plant, bioelectrochemistry device for producing hydrogen or PhotoelectrochemicalSystem System for Hydrogen Production device.
31. system ensembles according to claim 28, also comprise catalyzer, water or the steam reclaimed in described system ensemble, solid materials circulation device, and utilize the device of waste heat in described system ensemble or top pressure power generation or generation steam.
32. system ensembles according to claim 29, also comprise compound energy hydrogen manufacturing subsystem, and described compound energy hydrogen manufacturing subsystem is selected from hydrogen production plant by water electrolysis, biological hydrogen production plant, bioelectrochemistry device for producing hydrogen or PhotoelectrochemicalSystem System for Hydrogen Production device.
33. system ensembles according to claim 28, at least one in wherein said Poly-generation subsystem methanol, ethylene glycol.
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Families Citing this family (34)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101709227B (en) * | 2009-09-27 | 2015-05-06 | 新奥科技发展有限公司 | Comprehensive method and system for utilizing carbon-contained organic matter |
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| SE535702C2 (en) * | 2011-04-15 | 2012-11-13 | Reac Fuel Ab | Process for the treatment of organic material to produce methane gas |
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| CN117887774B (en) * | 2024-03-13 | 2024-05-28 | 山西牧禾农牧开发有限公司 | Process for producing ethanol and co-producing protein by fermenting carbon-containing solid waste by biological method and anaerobic cracking furnace |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1375447A (en) * | 2002-04-22 | 2002-10-23 | 西安交通大学 | Continuous supercritical water gasifying hydrogen producing method and apparatus with organic solid matter |
| CN1544580A (en) * | 2003-11-11 | 2004-11-10 | 中国科学院山西煤炭化学研究所 | Method for continuous conversion of low-rank coal in subcritical water or supercritical water |
| CN1654313A (en) * | 2005-01-17 | 2005-08-17 | 西安交通大学 | Coal-biomass co-overcritical water catalysis-gasification hydrogen production plant and method |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4664580B2 (en) * | 2003-07-18 | 2011-04-06 | 兵庫県 | Continuous processing equipment using subcritical water or supercritical water |
| CN101327908A (en) * | 2008-07-10 | 2008-12-24 | 中国兵器工业第五二研究所 | Method for using sludge in supercritical water for preparing hydrogen-rich gas by continuous catalysis gasification |
| CN101891149A (en) * | 2009-05-19 | 2010-11-24 | 新奥科技发展有限公司 | Continuous method for preparing combustible gas from high concentration slurry of carbon-containing organic matter |
| CN101709227B (en) * | 2009-09-27 | 2015-05-06 | 新奥科技发展有限公司 | Comprehensive method and system for utilizing carbon-contained organic matter |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1375447A (en) * | 2002-04-22 | 2002-10-23 | 西安交通大学 | Continuous supercritical water gasifying hydrogen producing method and apparatus with organic solid matter |
| CN1544580A (en) * | 2003-11-11 | 2004-11-10 | 中国科学院山西煤炭化学研究所 | Method for continuous conversion of low-rank coal in subcritical water or supercritical water |
| CN1654313A (en) * | 2005-01-17 | 2005-08-17 | 西安交通大学 | Coal-biomass co-overcritical water catalysis-gasification hydrogen production plant and method |
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