CN102453510B - Combined processing method of copyrolysis of heavy oil and coal - Google Patents
Combined processing method of copyrolysis of heavy oil and coal Download PDFInfo
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Abstract
A combined processing method of copyrolysis of heavy oil and coal comprises steps of: (1) introducing coal dust and heavy oil into a cracking reactor, contacting with high temperature coke powder from a gasification reactor for heating, generating a cracking reaction to obtain reacted oil gas and solid products of semicoke and coke powder, etc., carrying out gas-solid separation, introducing the reacted oil gas to a subsequent separating system for further separation and sending the semicoke and coke to the gasification reactor; (2) introducing a gasification medium containing water and oxygen into the gasification reactor, carrying out a gasification reaction on semicoke and coke from a cracker and water and oxygen to generate a synthetic gas and a high temperature coke powder; carrying out gas-solid separation and sending the high temperature coke powder to the cracking reactor to provide heat for the cracking reaction of coal and heavy oil. The method provided by the invention realizes combined production of coal cracking, heavy oil cracking and coal gasification, so as to substantially save energy consumption in coal cracking, heavy oil cracking and coal gasification.
Description
Technical field
The present invention relates to the combine production method of a kind of coal cracking and heavy oit pyrolysis.
Background technology
China is the country of oil-poor rich coal, and crude oil is heaviness, in poor quality increasingly, and the heavy component carbon residue in some crude oil and metal content are all very high, is difficult to efficiently it be fully utilized by traditional working method; Simultaneously, the coal resources of China are very abundant, and its workable reserves accounts for 49.6% of the world, and its metabituminous coal output accounts for 75% of national coal ultimate production.76% of China's energy consumption is coal at present, is mainly used in direct burning.Thereby wherein contained chemical resource can't be utilized effectively.
Gasification and gelatin liquefaction are by coal, to be made the important method of geseous fuel, synthetic gas and liquid fuel, also have in addition a kind of more economical method: dry distillation of coal method, and be about to the isolated air of coal and add the process that heat-flash makes its decomposition, also cry the coking of coal.Dry distillation of coal process mainly experiences following variation: when the temperature of coal charge during higher than 100 ℃, moisture in coal is evaporated, when temperature is elevated to more than 200 ℃, in coal, disengage in conjunction with water, up to more than 350 ℃ the time, caking coal starts to soften, and further forms the plastic mass (this phenomenon does not occur for mud coal, brown coal etc.) of thickness; To 400-500 ℃ of most of coal gas and tar, separate out, be called thermal decomposition product one time; At 450-550 ℃, thermolysis is proceeded, residue retrogradation solidify to form semicoke gradually; Higher than 550 ℃, semicoke continues to decompose, and separates out remaining volatile matter (main component is hydrogen) semicoke weightlessness and shrinks simultaneously, forms crackle; Temperature is higher than 800 ℃, and the hardening of semicoke volume-diminished forms porous coke.When destructive distillation was carried out in gas retort, one time thermal decomposition product contacted with red-hot coke and high temperature furnace wall, second heat occurs and decompose, and formed the second heat degradation production.
The destructive distillation final temperature is low-temperature pyrolysis lower than 700 ℃, and the destructive distillation final temperature is called coking or high temperature carbonization higher than 900 ℃.Low-temperature pyrolysis can obtain tar, coal gas and semicoke.High temperature carbonization mainly obtains coke.With raw coal, compare, the pollutent that semicoke contains is less than raw coal, favourable to environment protection.For units of heat, the coal tar oil and gas has higher economic worth than semicoke.Low-temperature pyrolysis coal tar is roughly similar with the character of coal Direct Hydrogenation liquefaction first stage gained oil plant, and the coal tar repeated hydrogenation is refining can obtain oil fuel, compares with liquefaction, and cost is relatively low.
Rich coal resources in China, raw coal is except part for coking, conversion processing, and the overwhelming majority is for directly burning.Coal is directly burnt, and not only thermo-efficiency is low, serious to the destruction of environment, and the hydrogen-rich component that has higher economic worth in coal can not get reasonable utilization.Therefore, the technological process that to develop coal conversion be clean fuel and multiple Chemicals has important practical significance.CNPC's shortage of resources, efficient, the comprehensive utilization of coal can reduce the dependence to Imported oil, Sweet natural gas to a certain extent.Therefore, before by raw coal combustion, make it under relatively mild condition, extract partially liq fuel and fine chemicals has great importance.For example, a kind of powder coal grading cleaning multigang utilization of pyrolysis as the first step of take disclosed in CN 101016482A, comprise raw coal processing preparation, pyrolysis, burning or gasification, pyrogenic processes is provided with Coal Chemical Industry isolation of purified system, wherein, raw coal enters pyrogenic processes with the fine coal of certain particle size and carries out pyrolysis after processing preparation, the gas-phase product after pyrolysis enters Coal Chemical Industry isolation of purified system, obtains hydro carbons Chemicals, the purified gas of high added value; The following selection of subsequent technique of the solid product semi-coke powder after pyrolysis: (1) enters the burning of burning operation, utilizes heat energy power-generating, heat supply; (2) enter the gasification process gasification, produce synthetic raw gas; (3) enter respectively simultaneously the burning of burning operation, gasification process gasification.
Processing the technique that mink cell focus is commonly used at present is delayed coking, and this technique is by making the mink cell focus thermally splitting obtain the products such as part coker gasoline, coker gas oil, coking distillate, hydrocarbon gas and coke.In this technique, because mink cell focus need at high temperature generate lighter oil product through the long time by thermally splitting, when the raw material carbon residue was very high, the green coke amount was very large.In order to address this problem, developed the heavy oil cracking technique that temperature of reaction is higher, the residence time is shorter.For example, CN 1504404A discloses the processing method that a kind of oil refining combines with gasification, and wherein, the method comprises the following steps: (1) petroleum hydrocarbon contacts, reacts with coke transfer agent in reactor; (2) separate the reaction oil gas generated and the coke transfer agent that reacts rear carbon deposit, reaction oil gas is sent into follow-up hydrocarbon products separation system, and the coke transfer agent of carbon deposit is delivered to vapourizing furnace after stripping; (3) in vapourizing furnace, the coke transfer agent of carbon deposit contacts with oxygen-containing gas with water vapor under gasification condition, to generate synthesis gas, the coke transfer agent of carbon deposit is regenerated; (4) coke transfer agent after step (3) regeneration returns in the described reactor of step (1) and recycles.
Yet, the method of disclosed coal cracking and heavy oil cracking all needs outside heat supply in above-mentioned two pieces of patent documentations, and the heat of the solid product produced in described coal cracking and heavy oil cracking process can not recycle, thereby causes heat recovery efficiency not high.
Summary of the invention
The above-mentioned defect that the present invention exists separately in order to overcome existing coal cleavage method and heavy oil cracking method, the combine production method of a kind of coal cracking and heavy oil cracking is provided, adopt the method can realize simultaneously coal cracking and heavy oil cracking, make simultaneously the solid product produced separately in coal cracking and heavy oil cracking process to recycle as thermal barrier, thereby greatly saved energy consumption.
The invention provides the combine production method of a kind of coal and heavy oil cracking, the method comprises the following steps:
(1) coal dust and heavy oil are introduced in cracking reactor, with the high temperature coke powder from gasifying reactor, contact intensification, scission reaction occurs obtain reaction oil gas and the solid products such as semicoke, coke powder, after gas solid separation, reaction oil gas is introduced subsequent separation system and is further separated, and semicoke and coke powder enter gasifying reactor;
(2) in gasifying reactor, introduce the gasifying medium that contains water and oxygen, semicoke and coke powder and water and oxygen reaction heat release from cracker, generate synthetic gas and high temperature coke powder, after gas solid separation, it is coal and heavy oit pyrolysis reaction heat supply that part high temperature coke powder returns to cracking reactor, another part rear discharger that fully gasifies.
In method provided by the invention, in step (1), the service temperature of cracking reactor is 400-700 ℃, and pressure is 0.1-20Mpa; The service temperature of the gasifying reactor in step (2) is 800-1200 ℃, and pressure is 0.1-20Mpa.
The beneficial effect of the combine production method of heavy oil provided by the invention and coal cracking is:
Heavy oit pyrolysis, coal dust cracking and three processes of coke powder gasification are combined, and form the mass transfer system of circulation.In cracker, coal dust mixes intensification with thermal barrier from gasifying reactor-high temperature coke powder, with the heavy oil that sprays into cracker, contact the generation scission reaction simultaneously.Heavy oil and coal cracking produce the solid products such as semicoke, coke powder, described solid product enters gasifying reactor and with the gasifying medium generating gasification, reacts the generation synthetic gas, in gasifying medium, contain oxygen, make in gasifying reactor the fully solid product of gasification burning heat release, obtain the high temperature coke powder and be circulated in described cracking reactor the scission reaction heat supply for coal and heavy oil.Therefore, the combine production method of coal provided by the invention and heavy oit pyrolysis has successfully been realized the combination producing of coal cracking, heavy oil cracking and gasification.Simultaneously, the solid product produced in coal cracking and heavy oit pyrolysis process recycles as thermal barrier, thereby has simplified flow process, and has greatly saved the energy consumption in the production process.
The accompanying drawing explanation
Accompanying drawing is the schematic flow sheet of the combine production method of coal provided by the invention and heavy oit pyrolysis.
Embodiment
As shown in drawings, the combine production method of heavy oil provided by the invention and coal cracking is so concrete enforcement, and the method comprises the following steps:
(1) coal dust and heavy oil are introduced in cracking reactor, with the high temperature coke powder from gasifying reactor, contact intensification, scission reaction occurs and obtain reaction oil gas and the solid products such as semicoke, coke powder, after gas solid separation, reaction oil gas is introduced subsequent separation system and is further separated; Isolated semicoke and coke powder enter gasifying reactor;
(2) in gasifying reactor, introduce the gasifying medium that contains water and oxygen, semicoke and coke powder and water and oxygen reaction heat release from cracker, generate the high temperature coke powder that synthetic gas and carbon (charcoal) content reduce, after gas solid separation, it is coal and heavy oit pyrolysis reaction heat supply that part high temperature coke powder returns to cracking reactor, another part rear discharger that fully gasifies.
In method provided by the invention, in step (1), as thermal barrier, provide heat for heavy oit pyrolysis in cracker and coal dust scission reaction from the high temperature coke powder of gasifying reactor.Cracking occurs in described heavy oil and coal dust under cracking condition, generating oil gas and take semicoke, coke powder is main solid product.
The cracking condition of described heavy oil and coal can suitably be selected in conventional heavy oil and coal crack reacting condition.Under preferable case, the service temperature of described cracker is 400-700 ℃, 450-600 ℃ more preferably, and pressure is 0.1-20MPa, 0.1-10MPa more preferably.In the present invention, described pressure refers to absolute pressure; The temperature of environment of living in when described cracker service temperature is heavy oil and contacts with thermal barrier with coal is also heavy oil and coal with after thermal barrier mixes, and the two occurs, and heat is transmitted and the temperature while reaching balance.
The service temperature of described cracker is carried out flexible by the amount of the high temperature coke powder of introducing cracker and the temperature of high temperature coke powder.In this case, the temperature of the high temperature coke powder by gasifying reactor is 800-1200 ℃, and the weight ratio of coal and described high temperature coke powder is 1: (1-10), be preferably 1: (2-8).The weight ratio of described mink cell focus and coal dust and high-temperature coke powder mixture is 1: (4-50), be preferably 1: (5-20).
In a preferred embodiment, for making the cracking more fully of heavy oil and coal dust, according to method provided by the invention also comprise make coal dust be heated to 100-350 ℃ before thermal barrier contacts.Mink cell focus was heated to 150-500 ℃ before entering cracking reactor, more preferably be heated to 200-450 ℃.
In method provided by the invention, described coal dust can be for having the various coals of conventional particle diameter, and under preferable case, the particle diameter of described coal dust is the 0.05-2 millimeter.Described coal dust is preferably at least a in peat, brown charcoal and bituminous coal.
In method provided by the invention, described heavy oil can be the mink cell focus of various routines, for example can be in oil, deasphalted oil, viscous crude and hydrocracking tail oil at the bottom of heavy crude, long residuum, normal pressure wax oil, vacuum residuum, wax tailings, tank at least a.
In method provided by the invention, step (1) can be implemented in the reactor of various routines, as long as this reactor can be realized the scission reaction of heavy oil and coal, therefore, cracker can be called cracking reactor.Described cracker is preferably the reactor of fluidized-bed reactor, riser reactor, down-flow reactor, moving-burden bed reactor or their array configuration.
In method provided by the invention, in step (2), under gasification condition, from solid products such as the semicoke of cracker and coke powders, with water vapor, contact the generating gasification reaction with oxygen, generate the coke powder that synthetic gas and carbon content reduce, described synthetic gas mainly contains hydrogen, carbon monoxide, lower carbon number hydrocarbons, carbonic acid gas and water.
Described gasification condition can suitably be selected in conventional gasification condition.Under preferable case, refer to that the service temperature of gasifying reactor is 800-1200 ℃, be preferably 800-1000 ℃, pressure is 0.1-20MPa, be preferably 0.1-10MPa.
Described gasifying medium is the gas that contains water vapour and oxygen, wherein, and the volume ratio 1-20 of water vapour and oxygen: 1.In gasifying reactor, pass into the amount of gasifying medium to guarantee to meet the gasification of the solid products such as semicoke and coke powder.The weight ratio of the amount of the solid product such as semicoke and coke powder, water vapor and oxygen is (2-5): (4-10): 1.
According to method provided by the invention, described water vapor and oxygen can add with the form of the mixed gas that contains water vapor and oxygen, and the temperature of described water vapor and oxygen can be 150-800 ℃, is preferably 200-600 ℃.
In method provided by the invention, step (2) can be implemented in the reactor of various routines, as long as this reactor can be realized the gasification reaction of semicoke and coke powder, therefore, gasifying reactor also can be called coal gasification reactor, and described coal gasification reactor for example can be fluidized-bed reactor.
The gaseous products such as the oil gas generated in cracker and gasifying reactor are with after solid product separates, method provided by the invention also comprises that the above-mentioned gas product is introduced to subsequent separation system further to be separated, and obtains heavy oil fraction, diesel oil distillate, gasoline fraction, water and splitting gas.The method of described separation can adopt conventional method to implement, and for example can, according to the difference of the condensing temperature of each different components, adopt separation column or adopt the mode of temperature control condensation to separate.
In method provided by the invention, to implementing separately separately described cracker and the separating of gaseous product that gasifying reactor produces.
Compared with prior art, the present invention has following advantage:
Coal dust cracking of the present invention and mink cell focus oil breaking, three of coke powder gasifications independently process combine, the semicoke of coal dust and heavy oit pyrolysis and coke powder etc. are introduced gasification in gasifying reactor and are produced synthetic gas, the high temperature coke powder that in gasifying reactor, temperature raises, carbon content reduces simultaneously returns to cracker as thermal barrier and recycles, the supplementary question of additional carrier and the problem that the external heat carrier separates with coke powder have been avoided, take full advantage of energy, reduced energy consumption.In addition, the common cracking of heavy oil and coal, can obtain the transformation efficiency of higher lightweight oil, lower carbon number hydrocarbons, hydrogen and carbon monoxide.
The following examples will be further described method provided by the invention, but not thereby limiting the invention.
Embodiment
Embodiment adopts flow process as shown in Figure 1, the coal dust (shown in table 1 composed as follows) that is the 0.3-2 millimeter by the particle diameter of 100 weight parts is heated to 200 ℃, then add in cracker, and mix with the high temperature coke powder (temperature is 900 ℃) from gasifier, to cracking reactor, spray into simultaneously 300 ℃ of heavy oil of 10 weight parts, heavy oil contacts with thermal barrier with coal dust to react and generates oil gas, semicoke and coke powder.Coal dust is 1: 5 with the weight ratio from the high temperature coke powder of gasifying reactor, is 550 ℃ by the temperature regulation of described cracker, and pressure is adjusted to 0.3MPa.
Semicoke, the coke powder (temperature is 550 ℃) of autothermic cracking device add in gasifier in the future, and inject wherein the mixed gas (temperature is 200 ℃) contain water vapor and oxygen, the weight ratio of described semicoke, coke powder and water vapor and oxygen is 3: 5: 1, semicoke and coke powder at high temperature generate the coke powder of synthetic gas and carbon content reduction with water vapour, oxygen reaction, heat release simultaneously heats up, and the temperature of regulating in gasifying reactor is 1000 ℃.The high temperature coke powder returns in cracker and recycles, the lime-ash discharger that gasification produces.
After the cyclonic separator gas solid separation, cracker is introduced to separation column with the gaseous product in gasifying reactor and separate.Coal dust (shanxi coal) character is in Table 1, and heavy oil (From Liaohe Heavy Crude) character is in Table 2, and reaction conditions and product composition are in Table 3, and the gas composition in table 3 is in Table 4, shown in the table 5 composed as follows of isolated synthetic gas the product of coal gasification reaction.
The composition of table 1 coal (wt%)
The character of table 2 heavy oil
| Project | |
| Density (20 ℃)/g.cm -3 | 1.07 |
| Kinematic viscosity (80 ℃)/mm 2·s -1 | 3648 |
| Carbon residue/wt% | 13.9 |
| Carbon content/wt% | 86.5 |
| Hydrogen richness/wt% | 10.9 |
| Sulphur content/wt% | 0.9 |
| Metal content/μ g.g -1 | 180 |
| Boiling range/℃ | |
| Initial boiling point | 263 |
| 5％ | 323 |
| 10％ | 361 |
| 30％ | 460 |
| 50％ | 530 |
Product and the yield of table 3 coal and heavy oit pyrolysis reaction
Table 4 splitting gas forms
| Splitting gas forms | wt％ |
| Methane | 10.2 |
| Ethane | 2.8 |
| Ethene | 1.9 |
| Propane | 1.8 |
| Propylene | 2.2 |
| C 4+Hydro carbons | 3.9 |
| Hydrogen | 0.9 |
| Carbonic acid gas | 53.6 |
| Carbon monoxide | 21.4 |
| Hydrogen sulfide | 1 |
| Nitrogen | 0.3 |
| Amount to | 100 |
Table 5 synthesis gas composition
| The composition of synthetic gas | Volume % |
| Methane | 2.1 |
| Hydrogen | 46.8 |
| Carbon monoxide | 32.8 |
| Carbonic acid gas | 18.3 |
| Amount to | 100 |
According to embodiment, can find out, adopt the combine production method of heavy oil provided by the invention and coal cracking to realize the combination producing of coal cracking, heavy oil cracking and gasification.
Claims (12)
1. the combined processing method of a heavy oil and coal copyrolysis, is characterized in that, comprises the following steps:
(1) coal dust and heavy oil are introduced in cracking reactor, with the high temperature coke powder from gasifying reactor, contact intensification, and scission reaction occurs obtain reaction oil gas and semicoke, coke powder solid product, after gas solid separation, reaction oil gas is introduced subsequent separation system and is further separated, and semicoke and coke powder enter gasifying reactor;
(2) in gasifying reactor, introduce the gasifying medium that contains water and oxygen, semicoke and coke powder from cracker react with water, oxygen generating gasification, generate synthetic gas and high temperature coke powder, after gas solid separation, it is coal and heavy oit pyrolysis reaction heat supply that the high temperature coke powder enters cracking reactor.
2. according to the method for claim 1, the service temperature that it is characterized in that cracking reactor described in step (1) is 400-700 ℃, and pressure is 0.1-20MPa.
3. according to the method for claim 2, the service temperature that it is characterized in that the cracking reactor described in step (1) is 450-600 ℃, and pressure is 0.1-10MPa.
4. according to claim 1,2 or 3 method, the weight ratio that it is characterized in that the coal dust described in step (1) and described high temperature coke powder is 1: (1-10), the weight ratio of described heavy oil and coal dust and high-temperature coke powder mixture is 1: (4-50).
5. according to the method for claim 4, the weight ratio that it is characterized in that the coal dust described in step (1) and described high temperature coke powder is 1: (2-8), the weight ratio of described heavy oil and coal dust and high-temperature coke powder mixture is 1: (5-20).
6. according to the method for claim 1, it is characterized in that the cracking reactor described in step (1) is selected from: the reactor of fluidized-bed reactor, riser reactor, down-flow reactor, moving-burden bed reactor and above-mentioned reaction one or more combination form.
7. according to the method for claim 1, the operational condition that it is characterized in that gasifying reactor described in step (2) is that temperature is 800-1200 ℃, and pressure is 0.1-20MPa.
8. according to the method for claim 7, the operational condition that it is characterized in that gasifying reactor described in step (2) is 800-1000 ℃, and pressure is 0.1-10MPa.
9. according to the method for claim 1, it is characterized in that described mink cell focus is selected from least a in oil at the bottom of heavy crude, long residuum, normal pressure wax oil, vacuum residuum, wax tailings, tank, deasphalted oil, viscous crude and hydrocracking tail oil.
10. according to the method for claim 1, it is characterized in that described coal dust is selected from: a kind of in peat, brown coal, bituminous coal or more than one mixture.
11., according to the method for claim 1, it is characterized in that described in step (2) that in gasifying medium, the volume ratio of water vapour and oxygen is (1-20): 1.
12., according to the method for claim 1, it is characterized in that the weight ratio of introducing semicoke, coke powder solid product, water vapour and oxygen in gasifying reactor in step (2) is (2-5): (4-10): 1.
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| CN104046373B (en) * | 2013-03-15 | 2016-12-28 | 中国石油化工股份有限公司 | The method being prepared bio-oil and synthesis gas by biomass |
| CN104046372A (en) * | 2013-03-15 | 2014-09-17 | 中国石油化工股份有限公司 | Method for preparing bio-oil and synthesis gas from biomass |
| CN103497786B (en) * | 2013-09-11 | 2015-04-15 | 陕西延长石油（集团）有限责任公司碳氢高效利用技术研究中心 | Method for preparing synthesis gas from dust coke |
| CN104312605A (en) * | 2014-09-23 | 2015-01-28 | 赵建勋 | Method for preparing combustible gas and active coke powder through pyrolysis |
| CN105586095B (en) * | 2014-10-22 | 2018-03-16 | 中国石油化工股份有限公司 | A kind of biomass microwave pyrolytic gasification reaction unit |
| CN113046129B (en) * | 2021-03-22 | 2023-02-03 | 邢彩虹 | Energy-saving kerosene co-refining method and device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4113602A (en) * | 1976-06-08 | 1978-09-12 | Exxon Research & Engineering Co. | Integrated process for the production of hydrocarbons from coal or the like in which fines from gasifier are coked with heavy hydrocarbon oil |
| CN1504404A (en) * | 2002-11-29 | 2004-06-16 | 中国石油化工股份有限公司 | Process combined oil refining and gasification |
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| CN1600831A (en) * | 2003-09-25 | 2005-03-30 | 田原宇 | Technique of solid phase heat carrier for recycle cracking heavy oil and gasification technique |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4113602A (en) * | 1976-06-08 | 1978-09-12 | Exxon Research & Engineering Co. | Integrated process for the production of hydrocarbons from coal or the like in which fines from gasifier are coked with heavy hydrocarbon oil |
| CN1504404A (en) * | 2002-11-29 | 2004-06-16 | 中国石油化工股份有限公司 | Process combined oil refining and gasification |
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