CN104498075B - A kind of Fast retrieval reactor and technique thereof - Google Patents
A kind of Fast retrieval reactor and technique thereof Download PDFInfo
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- CN104498075B CN104498075B CN201410800161.9A CN201410800161A CN104498075B CN 104498075 B CN104498075 B CN 104498075B CN 201410800161 A CN201410800161 A CN 201410800161A CN 104498075 B CN104498075 B CN 104498075B
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- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/085—Feeding reactive fluids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00893—Feeding means for the reactants
- B01J2208/00902—Nozzle-type feeding elements
Abstract
A kind of Fast retrieval reactor and technique thereof, the present invention relates to the pyrolysis of coal, solve existing pyrolytic process big energy-consuming, the problem that oily extraction yield is low.Reactor is provided with synthetic gas nozzle, hydrogen nozzle, coal nozzle, and temperature of reactor measuring point, and synthetic gas nozzle is communicated with Sweet natural gas, oxygen intake pipe, and synthetic gas nozzle is also communicated with cooling water intakeoutfall; Quench tank is communicated with the bottom of reactor, and Quench tank is connected with water inlet, water outlet, and Quench tank is provided with cooling water nozzle, Quench tank temperature point, shock chamber's outlet.Present invention process step: first synthetic gas is sent into reactor, under an atmosphere of hydrogen, pulverized coal conveying generation fast pyrogenation reacts, and then desuperheat makes reaction terminating rapidly.The present invention is used for coal liquifaction field, has that structure is simple, consume energy low, that coal transformation efficiency is high, oil product productive rate is high advantage.
Description
Technical field
The invention belongs to coal liquifaction field, be specifically related to the pyrolysis oven of coal, particularly a kind of Fast retrieval entrained-flow reactor and technique thereof.
Background technology
The energy is the basis of the national economic development, and the feature of China's energy structure is " rich coal, weak breath, oil starvation ".At present, the prospective oil that China has been verified is 24,800,000,000 tons, natural gas reserves 4.4 trillion m
3, coal reserves is more than 1,000,000,000,000 tons.2011, the coal that China produces was 35.2 hundred million tons, crude oil 2.01 hundred million tons, Sweet natural gas 1011.15 hundred million m
3, consumption of coal accounts for more than 70% of overall energy expenditure.From reserves data, coal, in China's energy consumption structure, will be occupied an leading position for a long time.From following China energy consumption structure trend, Coal Energy Source consumption proportion will reduce year by year, and oil, natural gas consumption ratio will increase year by year, cause oil supply external dependence degree can increase year by year (within 2011, reaching 56.5%).By modern coal liquifaction technology, being various oil product and Chemicals by coal conversion, is the Strategic Measure meeting China's energy consumption structure feature.
At present, domestic coal liquifaction technology is mainly with direct liquefaction or indirect liquefaction.Direct liquefaction reaction conditions is relatively harsh, Germany old process liquefaction pressure even up to 70MPa, modern crafts also at 17 ~ 30MPa, liquefaction temperature 420 ~ 470 DEG C.Coal narrow application range, direct liquefaction is mainly applicable to the Young Coals such as brown coal, long-flame coal, bottle coal, non-caking coal, weakly caking coal.The product composition going out liquefying reactor is complicated, and liquid, solid two-phase mixture are higher due to viscosity, are separated relatively difficulty.Hydrogen consumption is large, generally 6 ~ 10%, not only will supplement a large amount of new hydrogen, also need turning oil to make hydrogen supply dissolvent, the throughput of device is reduced in technological process.Indirect liquefaction oil yield is low, and reactant is gas phase, and equipment volume is huge, and invest high, working cost is high; The selectivity of target product is lower, and synthesising by-product is more; The scope of positive structure chain hydrocarbon from C1 ~ C100, can reduce with synthesis temperature, and heavy hydrocarbons output increases, and light hydrocarbon output reduces.
Summary of the invention
Object of the present invention is intended to the shortcoming overcoming prior art existence, provides a kind of Fast retrieval reactor and technique thereof, solves the direct liquefaction technique of current coal liquifaction technology, and water consumption, hydrogen-consuming volume are large, and equipment capacity is low; Indirect liquefaction technique, the extraction yield of oil is low, facility investment technical problem costly.
The present invention is achieved by the following technical solutions:
A kind of Fast retrieval reactor, be made up of reactor and Quench tank two portions, the casing lining refractory materials of described reactor, synthetic gas nozzle is installed at the top of described reactor, hydrogen nozzle is installed in middle and upper part, coal nozzle is installed in middle and lower part, the middle part of described reactor and bottom are equipped with temperature of reactor measuring point respectively, described synthetic gas nozzle is communicated with Sweet natural gas inlet pipe, oxygen intake pipe, and described synthetic gas nozzle is also communicated with entrance of cooling water, cooling water outlet; Described Quench tank is communicated with the bottom of described reactor, described Quench tank is connected with water-in, water outlet, forms built-in water-cooling wall construction, and Quench nozzle is installed on described Quench tank top, Quench tank temperature point is equipped with at the middle part of described Quench tank, and the bottom of described Quench tank is shock chamber's outlet.
Further, described coal nozzle is symmetrical, nozzle number 2 ~ 4, and described coal nozzle is 0 ~ 10 degree along the angle of reactor furnace wall tangential direction.
Further, the angle of described coal nozzle and synthetic gas nozzle centerline is 30 ~ 150 degree.
Further, described hydrogen nozzle is symmetrical, and nozzle number is 2 ~ 4, and the angle of described hydrogen nozzle and synthetic gas nozzle centerline is 30 ~ 60 degree.
A kind of pyrolytic reaction processing step of Fast retrieval reactor is:
A, first form synthetic gas by Sweet natural gas, oxygen, send into reactor combustion through synthesis gas jets, produces 1300 ~ 1500 DEG C of high temperature, meanwhile, through the hydrogen feeding reactor that hydrogen nozzle will be recycled;
B, by raw coal send into grinding and dehumidification system, obtain granularity 5 ~ 90 microns, moisture 2 ~ 3%, the coal dust that temperature is 105 ~ 110 DEG C;
C, coal dust send into reactor through pressure conveyer device, and under an atmosphere of hydrogen, coal dust generation fast pyrogenation reacts, temperature of reactor 800 ~ 1000 degree, pressure 3.0 ~ 5.0MPa, and the reaction process residence time is less than 1S;
D, reactant enter Quench tank, rapid desuperheat to 500 ~ 600 degree, reaction terminating;
E, gas-solid mixture are exported by shock chamber and enter high temperature cyclone separator, isolate 98% half defocused, then to filter through high temperature fly-ash filter, pressure 3.0 ~ 5.0MPa, temperature about 500 DEG C, dust content is less than 10mg/m3, thus obtains the oil product that dustiness is less than 0.1% dust content.
Further, in step C the transfer pressure of pressure conveyer device higher than reactor 8 ~ 15bag.
The present invention compared with prior art, has the following advantages and beneficial effect:
1, oil yield rate is high: essence of the present invention is proposed to be converted into liquid product in large for volatile matter original in feed coal portion, and namely in moment temperature raising situation, the various bridged bonds of coal rupture instantaneously, form the free radical of extremely unstable.In hydrogen atmosphere, the free hydrogen produced makes pyrolysis of coal product and the further pyrogenous origin macromole group of coal settle out (light hydrocarbon gas, gas phase fragrancing liquid, gas phase portion saturated liquid, vapour phase BTX, oxycarbide), facilitate the formation (namely facilitating macromolecular hydrocarbon cracking is small molecule hydrocarbon reaction) of low molecule product, slow down the process (namely hindering the polycondensation that macromole is mutual) that thermal polycondensation generates solid product.Meanwhile, be oxidized the H2 obtained, participate in conversion reaction, add efficiency of carbon conversion, also improve the productive rate of product liquid simultaneously from CH4 in self-produced carbonization gas, therefore, oil yield rate of the present invention is relatively high.
2, water loss is few: in traditional technology, water loss is mainly recirculated cooling water and participates in the water of technological reaction, and the water participating in technological reaction mainly reacts Formed oxide compound and H2 with semicoke; And the whole polycondensation of this part carbon is converted into product char in the present invention, do not participate in reacting with water, and H2 of the present invention is from CH4 oxidation in self-produced carbonization gas, participate in being obtained by reacting H2 without the need to water, therefore, water consumption of the present invention is only recirculated cooling water, and water loss is less.
3, CO2 discharge is low: due to the anhydrous participation reaction of present invention process process, decrease the generation (especially CO2) of oxycarbide; And whole technological process is a reduction process (as hydrogenation or interpolation hydrogen molecule), instead of produce the oxidising process (interpolation oxygen) of CO2 major cause, therefore, CO2 discharge of the present invention is low.
4, in solid semicoke, sulphur content is low: in coal, sulphur content is organosulfur and inorganic sulfur, inorganic sulfur very easily removes, and the organosulfur form that difficulty removes is generally fatty sulphur and thiophenic sulfur, and Fast retrieval can remove whole fatty sulphur and part thiophenic sulfur, therefore, in semicoke of the present invention, sulphur content is low.
5, facility investment expense is few: catalyzer is the core technology of DCL/Direct coal liquefaction process, play very important effect, also to there is Meteorological, conventional operation cost (periodic replacement), problem that post-processed expense (environmental problem) is high while oil yield rate improving, the present invention is to catalyzer not too much requirement, therefore, facility investment expense of the present invention is low.
The present invention is used for coal liquifaction field, has that structure is simple, consume energy low, that coal transformation efficiency is high, oil product productive rate is high, facility investment is few advantage.
Accompanying drawing explanation
Fig. 1 is a kind of structural representation of Fast retrieval reactor;
Fig. 2 is coal nozzle scheme of installation, and wherein 1,2,4 is 2 ~ 4 coal nozzle orientation sketches, and 3 is that coal nozzle is along reactor tangent line angle of rotation schematic diagram;
Fig. 3 is the process matched therewith general flow chart of reactor.
Embodiment
The exemplary embodiments embodying feature & benefits of the present invention will describe in detail by reference to the accompanying drawings in the following description.The present invention can have various change in different embodiments, neither departs from protection scope of the present invention, explanation wherein and to be shown in be when the use that explain in essence, and is not used to limit the present invention.
As shown in Figure 1, a kind of Fast retrieval reactor, be made up of reactor 1 and Quench tank 2 two portions, housing 11 inner lining refractory 111 of described reactor 1, synthetic gas nozzle 12 is installed at the top of described reactor 1, hydrogen nozzle 131/132/13X is installed in middle and upper part, coal nozzle 141/142/14X is installed in middle and lower part, middle part and the bottom of described reactor 1 are equipped with temperature of reactor measuring point 15 respectively, described synthetic gas nozzle 12 and Sweet natural gas inlet pipe 121, oxygen intake pipe 122 is communicated with, described synthetic gas nozzle 12 also with entrance of cooling water 123, cooling water outlet 124 is communicated with, described Quench tank 2 is communicated with the bottom of described reactor 1, described Quench tank 2 is connected with water-in 21, water outlet 22, form built-in water-cooling wall construction, heat is recycled fully, Quench nozzle 231/232 (can adopt water Quench or gas Quench) is installed on described Quench tank 2 top, Quench tank temperature point 24 is equipped with at the middle part of described Quench tank 2, and the bottom of described Quench tank 2 is shock chamber's outlet 25.
The angle of described coal nozzle 141/142/14X and synthetic gas nozzle 12 medullary ray is 30 ~ 150 degree, mainly to the recycling of tail gas hydrogen, ensures that coal dust enters the stationarity of burner hearth temperature of reaction and provides part hydrogen source to the hydrogen atmosphere in burner hearth.
Described hydrogen nozzle 131/132/13X is symmetrical, and nozzle number is 2 ~ 4, and the angle of described hydrogen nozzle 131/132/13X and synthetic gas nozzle 12 medullary ray is 30 ~ 60 degree.
As shown in Figure 2, described coal nozzle 141/142/14X is symmetrical, and nozzle number is 2 ~ 4, and described coal nozzle 141/142/14X is 0 ~ 10 degree along the angle β of reactor furnace wall tangential direction.
Shown in Fig. 1,3, a kind of pyrolytic reaction processing step of Fast retrieval reactor is:
A, first form synthetic gas by Sweet natural gas, oxygen, send into reactor 1 combustion through synthesis gas jets 12, produces 1300 ~ 1500 DEG C of high temperature, meanwhile, through the hydrogen feeding reactor 1 that hydrogen nozzle 131/132/13X will recycle;
B, by raw coal send into grinding and dehumidification system, obtain granularity 5 ~ 90 microns, moisture 2 ~ 3%, the coal dust that temperature is 105 ~ 110 DEG C;
C, coal dust send into reactor 1 through pressure conveyer device, and under an atmosphere of hydrogen, coal dust generation fast pyrogenation reacts, temperature of reactor 800 ~ 1000 degree, pressure 3.0 ~ 5.0MPa, and the reaction process residence time is less than 1S;
D, reactant enter Quench tank 2, rapid desuperheat to 500 ~ 600 degree, reaction terminating;
E, gas-solid mixture are exported by shock chamber and 25 enter high temperature cyclone separator, isolate 98% half defocused, then to filter through high temperature fly-ash filter, pressure 3.0 ~ 5.0MPa, temperature about 500 DEG C, dust content is less than 10mg/m3, thus obtains the oil product that dustiness is less than 0.1% dust content.
In step C, the transfer pressure of pressure conveyer device is higher than reactor 8 ~ 15bag.
As shown in Figure 3, the process matched therewith flow process of reactor is as follows:
From Sweet natural gas oxidation high-temperature synthesis gas mix with recover hydrogen after, react in reactor with the coal dust of delivery system, the gas-solid mixture after Quench enters decoking operation, and after gas solid separation, gas phase enters oil gas cooling system, solid phase enter burnt tank recycling.After oil gas refrigerated separation, by oil classification process, gas sweetening is recycled, non-serviceable feeding torch.Native system water consumption is few, waste water is sent into water treatment device and recycles.
Although with reference to exemplary embodiment describing structure of the present invention, term used to illustrate and exemplary and nonrestrictive.The spirit of invention is not departed from because the present invention can specifically implement in a variety of forms, so be to be understood that above-described embodiment is not limited to aforesaid details, and should explain widely in claim limited range, therefore fall into the change in claim or its equivalent scope and remodeling, all should be claim and contained.
Claims (5)
1. a Fast retrieval reactor, it is characterized in that: described Fast retrieval reactor is made up of reactor (1) and Quench tank (2) two portions, housing (11) inner lining refractory (111) of described reactor (1), synthetic gas nozzle (12) is installed at the top of described reactor (1), hydrogen nozzle (131/132/13X) is installed in middle and upper part, coal nozzle (141/142/14X) is installed in middle and lower part, the middle part of described reactor (1) and bottom are equipped with temperature of reactor measuring point (15) respectively, described synthetic gas nozzle (12) and Sweet natural gas inlet pipe (121), oxygen intake pipe (122) is communicated with, described synthetic gas nozzle (12) also with entrance of cooling water (123), cooling water outlet (124) is communicated with, described Quench tank (2) is communicated with the bottom of described reactor (1), described Quench tank (2) is connected with water-in (21), water outlet (22), form built-in water-cooling wall construction, Quench nozzle (231/232) is installed on described Quench tank (2) top, Quench tank temperature point (24) is equipped with at the middle part of described Quench tank (2), and the bottom of described Quench tank (2) is shock chamber's outlet (25).
2. Fast retrieval reactor according to claim 1, it is characterized in that: described coal nozzle (141/142/14X) is symmetrical, nozzle number is 2 ~ 4, and described coal nozzle (141/142/14X) is 0 ~ 10 degree along the angle (β) of reactor furnace wall tangential direction.
3. Fast retrieval reactor according to claim 1 and 2, is characterized in that: described coal nozzle (141/142/14X) is 30 ~ 150 degree with the angle of synthetic gas nozzle (12) medullary ray.
4. Fast retrieval reactor according to claim 1, it is characterized in that: described hydrogen nozzle (131/132/13X) is symmetrical, nozzle number is 2 ~ 4, and described hydrogen nozzle (131/132/13X) is 30 ~ 60 degree with the angle of synthetic gas nozzle (12) medullary ray.
5. the pyrolytic reaction technique of Fast retrieval reactor according to claim 1, is characterized in that: described processing step is:
A, first form synthetic gas by Sweet natural gas, oxygen, reactor (1) combustion is sent into through synthesis gas jets (12), produce 1300 ~ 1500 DEG C of high temperature, meanwhile, through hydrogen nozzle (131/132/13X), the hydrogen recycled is sent into reactor (1);
B, by raw coal send into grinding and dehumidification system, obtain granularity 5 ~ 90 microns, moisture 2 ~ 3%, the coal dust that temperature is 105 ~ 110 DEG C;
C, coal dust send into reactor (1) through pressure conveyer device, and under an atmosphere of hydrogen, coal dust generation fast pyrogenation reacts, temperature of reactor 800 ~ 1000 degree, pressure 3.0 ~ 5.0MPa, and the reaction process residence time is less than 1S;
D, reactant enter Quench tank (2), rapid desuperheat to 500 ~ 600 degree, reaction terminating;
E, gas-solid mixture export (25) by shock chamber and enter high temperature cyclone separator, isolate 98% half defocused, filter through high temperature fly-ash filter again, pressure 3.0 ~ 5.0MPa, temperature 500 DEG C, dust content is less than 10mg/m3, thus obtains the oil product that dustiness is less than 0.1% dust content.
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| CN104762107B (en) * | 2015-04-20 | 2017-10-24 | 新奥科技发展有限公司 | Entrained flow bed gasification system and entrained flow gasification technique |
| CN104946292B (en) * | 2015-06-08 | 2016-08-17 | 中美新能源技术研发（山西）有限公司 | A kind of fine coal hydropyrolysis to-oil reactor and technique |
| CN106986747B (en) * | 2017-04-19 | 2020-10-09 | 中美新能源技术研发（山西）有限公司 | Integrated process for preparing methanol by pyrolyzing pulverized coal with natural gas |
| TWI754084B (en) * | 2017-08-03 | 2022-02-01 | 日商荏原製作所股份有限公司 | Exhaust gas treatment apparatus |
| CN114181741B (en) * | 2021-11-19 | 2022-09-20 | 新奥科技发展有限公司 | Coal hydro-gasification device |
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| SU1666513A1 (en) * | 1989-04-06 | 1991-07-30 | Государственный Энергетический Институт Им.Г.М.Кржижановского | Jet reactor for high-speed pyrolysis of powdered solids |
| JP2853916B2 (en) * | 1991-06-06 | 1999-02-03 | 新日本製鐵株式会社 | Apparatus and method for rapid pyrolysis of coal |
| CN1125159C (en) * | 2000-10-09 | 2003-10-22 | 王逢旦 | Quick hydrogen cracking coal method and equipment therefor |
| WO2011129243A1 (en) * | 2010-04-16 | 2011-10-20 | 新日鉄エンジニアリング株式会社 | Operational method for coal gasification reaction furnace and coal gasification reaction furnace |
| CN202744505U (en) * | 2012-09-04 | 2013-02-20 | 新奥科技发展有限公司 | Chiller and gasification furnace with same |
| CN203700291U (en) * | 2013-11-19 | 2014-07-09 | 中国科学院山西煤炭化学研究所 | Gasification furnace for synthetic natural gas |
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