CN102382667B - Coal cracking and heavy oil cracking joint production method - Google Patents
Coal cracking and heavy oil cracking joint production method Download PDFInfo
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Abstract
The invention discloses a coal cracking and heavy oil cracking joint production method, which comprises the following steps of: (1) contacting coal with a first heat carrier under the coal cracking condition to obtain a first solid product and a first gas product; (2) contacting heavy oil with a second heat carrier under the heavy oil cracking condition to obtain a second solid product and a second gas product, wherein the second heat carrier comprises the first solid product; and (3) contacting the second solid product with water vapor and oxygen under the coal gasifying condition to obtain a third solid product and a third gas product, wherein the first heat carrier and/or the second heat carrier comprises the third solid product. By adopting the method provided by the invention, joint production of coal cracking, heavy oil cracking and coal gasifying is realized, and energy consumption in the coal cracking, heavy oil cracking and coal gasifying processes is lowered greatly.
Description
Technical field
The present invention relates to the combine production method of a kind of coal cracking and heavy oil cracking.
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, by traditional working method, is difficult to efficiently it be fully utilized; 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 to be made the important method of geseous fuel, synthetic gas and liquid fuel by coal, also have in addition a kind of more economical method: dry distillation of coal method.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, with liquefaction, compares, 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 that pyrolysis is the first step of take is 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, and 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 subsequent technique of the solid product semi-coke powder after pyrolysis is selected as follows: (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 the burning of burning operation, gasification process gasification simultaneously.
Processing mink cell focus technique 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 longer time by thermally splitting, when the raw material carbon residue is very high, the green coke amount is 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, makes the coke transfer agent of carbon deposit be regenerated simultaneously; (4) coke transfer agent after step (3) regeneration returns in the described reactor of step (1) and recycles.
Yet, in above-mentioned two pieces of patent documentations, the method for disclosed coal cracking and heavy oil cracking all needs outside heat supply, 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 coal cracking and heavy oil cracking simultaneously, make the solid product produced separately in coal cracking and heavy oil cracking process to recycle as thermal barrier simultaneously, thereby greatly saved energy consumption.
The invention provides the combine production method of a kind of coal cracking and heavy oil cracking, the method comprises: (1), under the condition of coal cracking, makes coal contact with the first thermal barrier, obtains the first solid product and the first gaseous product; (2) under the condition of heavy oil cracking, mink cell focus is contacted with the second thermal barrier, obtain the second solid product and the second gaseous product, the second thermal barrier comprises the first solid product; (3) under the condition of gasification, the second solid product is contacted with oxygen with water vapor, obtain the 3rd solid product and the 3rd gaseous product; And the first thermal barrier and/or the second thermal barrier comprise the 3rd solid product.
The combine production method of coal cracking according to the present invention and heavy oil cracking, by coal cracking, heavy oil cracking and gasification Four processes are combined, and the mass transfer system of formation circulation, the solid product that makes the coal cracking produce can enter in the heavy oil cracking reactor, as the thermal barrier of heavy oil cracking reaction; And the solid product that heavy oil cracking produces can enter in coal gasification reactor and contacts with oxygen with water vapor, thereby generation coal gasification reaction, the solid product produced due to heavy oil cracking with understand the generation thermopositive reaction after oxygen contact, make the solid product fully do not gasified in coal gasification reactor absorb in this thermopositive reaction and produce heat, thereby there is higher temperature; By the described solid product fully do not gasified is circulated in described coal cracking reactor and/or heavy oil cracking reactor, to described coal cracking reactor and/or heavy oil cracking reactor, to provide heat.Therefore, successfully realized the combination producing of coal cracking, heavy oil cracking and gasification according to the combine production method of coal cracking provided by the invention and heavy oil cracking; Simultaneously, make the solid product produced in each comfortable coal cracking and heavy oil cracking process to recycle as thermal barrier, thereby greatly saved the energy consumption in the production process.
The accompanying drawing explanation
Fig. 1 means the schema according to the production process of the embodiment of the present invention 1 and 2;
Fig. 2 means the schema according to the production process of the embodiment of the present invention 3.
Embodiment
According to the combine production method of coal cracking of the present invention and heavy oil cracking, comprise the following steps:
(1) under the condition of coal cracking, coal is contacted with the first thermal barrier, obtain the first solid product and the first gaseous product;
(2) under the condition of heavy oil cracking, mink cell focus is contacted with the second thermal barrier, obtain the second solid product and the second gaseous product, the second thermal barrier comprises the first solid product;
(3) under the condition of gasification, the second solid product is contacted with oxygen with water vapor, obtain the 3rd solid product and the 3rd gaseous product; And the first thermal barrier and/or the second thermal barrier comprise the 3rd solid product.
In step (1), coal is under the effect of the first thermal barrier, and the temperature of described coal raises and cracking occurs, and discharges most of volatile wherein, thereby the split product obtained comprises gaseous product and solid product, be also the first gaseous product and the first solid product.Described the first solid product mainly comprises semicoke and coke powder, and described semicoke is mainly produced by the coal scission reaction, and described coke powder is mainly from the thermal barrier entered in described the first reactor.Described the first gaseous product mainly comprises the coal tar oil and gas.
According to 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 coal scission reaction, therefore, this reactor can be called the coal cracking reactor.Described coal cracking reactor can be for example the reactor of fluidized-bed reactor, riser reactor, down-flow reactor, moving-burden bed reactor or their array configuration.In the present invention, described the first solid product refers to the solid product of discharging from the coal cracking reactor, and described the first gaseous product refers to expellant gas product from the coal cracking reactor.
In step (2), mink cell focus is under the effect of the second thermal barrier, the temperature of described mink cell focus raises rapidly, atomization occurs, mink cell focus generation heat scission reaction after atomization simultaneously, thereby the split product obtained comprises gaseous product and solid product, be also the second gaseous product and the second solid product.Described the second solid product mainly comprises the coke powder particle, and described the second gaseous product mainly comprises reacted gas, gasoline fraction, diesel oil distillate and heavy oil fraction.
According to 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 heavy oil cracking reaction, therefore, this reactor can be called the heavy oil cracking reactor.Described heavy oil cracking reactor can be for example the reactor of fluidized-bed reactor, riser reactor, down-flow reactor or their array configuration.In the present invention, described the second solid product refers to the solid product of discharging from the heavy oil cracking reactor, and described the second gaseous product refers to expellant gas product from the heavy oil cracking reactor.
In step (3), under the condition of gasification, contacting to occur coal gasification reaction with oxygen with water vapor by the solid product that the heavy oil cracking reaction is produced, thereby generate solid product and gaseous product, is also the 3rd solid product and the 3rd gaseous product.Described the 3rd solid product mainly contains not the fully coke powder particle of gasification, and described the 3rd gaseous product mainly contains hydrogen, carbon monoxide, lower carbon number hydrocarbons, carbonic acid gas and water.
According to method provided by the invention, step (3) can be implemented in the reactor of various routines, as long as this reactor can be realized coal gasification reaction, therefore, this reactor can be called coal gasification reactor, and described coal gasification reactor can be for example fluidized-bed reactor.In the present invention, described the 3rd solid product refers to the solid product of discharging from coal gasification reactor, and described the 3rd gaseous product refers to expellant gas product from coal gasification reactor.
A preferred embodiment of the invention, described the first thermal barrier is the 3rd solid product, described the second thermal barrier is the first solid product.
According to another kind of preferred implementation of the present invention, described the first thermal barrier is the 3rd solid product, the mixture that described the second thermal barrier is the first solid product and the 3rd solid product.In this case, in the second thermal barrier, the weight ratio of the first solid product and the 3rd solid product is 1: 0.1-10 is preferably 1: 0.2-5.
In above two kinds of preferred implementations, in the reaction of coal scission reaction and heavy oil cracking, can obtain the higher transformation efficiency that is converted into lightweight oil, lower carbon number hydrocarbons, hydrogen and carbon monoxide by coal and mink cell focus.
According to method provided by the invention, the condition of described coal cracking can suitably be selected in conventional coal crack reacting condition.Under preferable case, the condition of described coal cracking comprises that the temperature that coal contacts with the first thermal barrier is 450-700 ℃, more preferably 450-650 ℃.In this case, the temperature of the first thermal barrier is 800-1200 ℃, and the weight ratio of coal and this first thermal barrier is 1: 1-10 is preferably 1: 2-8.Under further preferable case, the condition of described coal cracking also comprises that the pressure that coal contacts with the first thermal barrier is 0.1-0.6MPa, more preferably 0.1-0.4MPa.In the present invention, described pressure refers to absolute pressure; The temperature that described coal contacts with the first thermal barrier refers to the temperature of environment of living in when coal contacts with the first thermal barrier, is also coal with after the first thermal barrier mixes, and the two occurs, and heat is transmitted and the temperature while reaching balance.
In a kind of preferred implementation, for making coal cracking more fully, according to method provided by the invention also comprise make coal be heated to 100-350 ℃ before the first thermal barrier contacts.
In the present invention, described coal can be for having the various coals of conventional particle diameter, and under preferable case, the particle diameter of described coal is the 0.05-2 millimeter.Described coal can be for example at least one in peat, brown charcoal and bituminous coal.
According to method provided by the invention, the condition of described heavy oil cracking can suitably be selected in conventional heavy oil cracking reaction conditions.Under preferable case, the condition of described heavy oil cracking comprises that the temperature that mink cell focus contacts with the second thermal barrier is 450-650 ℃, more preferably 450-550 ℃.In this case, in the second thermal barrier, the temperature of the first solid product is 450-700 ℃, and the temperature of the 4th solid product is 800-1200 ℃, and the weight ratio of described mink cell focus and the second thermal barrier is 1: 4-50 is preferably 1: 5-20.Under further preferable case, the condition of described heavy oil cracking also comprises that the pressure that mink cell focus contacts with the second thermal barrier is 0.1-0.6MPa, more preferably 0.1-0.4MPa.The temperature that described mink cell focus contacts with the second thermal barrier refers to the temperature of environment of living in when mink cell focus contacts with the second thermal barrier, is also mink cell focus with after the second thermal barrier mixes, and the two occurs, and heat is transmitted and the temperature while reaching balance.
In a kind of preferred implementation, for making mink cell focus cracking more fully, according to method provided by the invention also comprise make mink cell focus be heated to 150-500 ℃ before the second thermal barrier contacts, more preferably be heated to 200-450 ℃.
In the present invention, described mink cell focus can be the mink cell focus of various routines, can be for example at least one 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.
According to method provided by the invention, the condition of described gasification can suitably be selected in conventional gasification condition.Under preferable case, the condition of described gasification comprises that the temperature that the second solid product contacts with oxygen with water vapor is 800-1200 ℃, is preferably 800-1000 ℃.In this case, the temperature of the second solid product can be 450-650 ℃, and the weight ratio of the second solid product, water vapor and oxygen is 2-5: 4-10: 1.Under further preferable case, the condition of described gasification also comprises that the pressure that described material contacts with oxygen with water vapor is 0.1-0.6MPa, is preferably 0.1-0.4MPa.
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 300-600 ℃.
Under above-mentioned gasification condition, the particle diameter of the solid product (i.e. the 3rd solid product) produced after the second solid product contacts with oxygen with water vapor is preferably the 0.01-3 millimeter.
According to one embodiment of the present invention, described method can also comprise is separated with described the second gaseous product described the first gaseous product, to be separated into heavy oil fraction, diesel oil distillate, gasoline fraction, water and 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 the mode of temperature control condensation to be separated.
In the present invention, to described the first gaseous product and separating of described the second gaseous product, can implement separately separately, implement together again after also the two can being converged to separate.Consider production cost, implement together again after preferably the two being converged to separate.
According to one embodiment of the present invention, described method can also comprise discharges described the second solid product of part, and the cooling coke powder product to obtain, and makes described second solid product of other parts carry out coal gasification reaction simultaneously.The amount of discharging and carrying out cooling described the second solid product can, for the 5-60 % by weight of the gross weight of described the second solid product, be preferably the 20-50 % by weight.
The present invention is further detailed explanation by the following examples.
Embodiment 1
The present embodiment is for illustrating the combine production method of described coal cracking provided by the invention and heavy oil cracking.
As shown in Figure 1, the coal dust that is the 0.3-2 millimeter by the particle diameter of 100 weight parts (shown in table 1 composed as follows) is heated to 200 ℃, then add in the coal cracking reactor, and (temperature is 900 ℃ with the 3rd solid product from coal gasification reactor, particle diameter is the 0.05-3 millimeter) mix, the weight ratio that makes coal dust and the 3rd solid product is 1: 4, thereby is 580 ℃ by the temperature regulation of described coal cracking reactor, and pressure is adjusted to 0.3MPa.After processing, the coal cracking reactor obtains gaseous product and solid product, i.e. the first gaseous product and the first solid product.
The heavy crude of 10 weight parts (shown in table 2 composed as follows) is heated to 200 ℃, then add in the heavy oil cracking reactor, and mix with the first solid product (temperature is 550 ℃) from the coal cracking reactor, making heavy crude in described heavy oil cracking reactor and the weight ratio of described the first solid product is 1: 8, thereby by the temperature regulation of described heavy oil cracking reactor, be 500 ℃, pressure is adjusted to 0.3MPa.Obtain gaseous product and solid product after the heavy oil cracking reactor for treatment, i.e. the second gaseous product and the second solid product.
To add in coal gasification reactor from second solid product (temperature is 480 ℃) of heavy oil breaking reactor, and the mixed gas (temperature is 200 ℃) that injection contains water vapor and oxygen wherein, so that this second solid product generation coal gasification reaction, the weight ratio of described the second solid product, water vapor and oxygen is 3: 6: 1, thereby is 1000 ℃ by the temperature regulation in described coal gasification reactor.After processing, coal gasification reactor obtains gasification product and solid product, i.e. third product component and the 3rd solid product.Make the solid product produced in described coal gasification reactor be circulated in described coal cracking reactor simultaneously.
For convenience of operation, described the first gaseous product and described the second gaseous product are converged, and adopt the mode of temperature control condensation to be separated.Table 3 is that coal scission reaction and heavy oil cracking react product and the yield thereof while reaching material balance, and coal gasification reaction produces the yield of synthetic gas, and in table 3 from the product of coal scission reaction and heavy oit pyrolysis reaction shown in the table 4 composed as follows of isolated gas, from the product of coal gasification reaction shown in the table 5 composed as follows of isolated synthetic gas.
Table 1
Table 2
| Project | |
| Density (20 ℃)/g.cm -3 | 1.07 |
| Kinematic viscosity (80 ℃)/mm 2·s -1 | 3648 |
| Carbon residue/% by weight | 13.9 |
| Carbon content/% by weight | 86.5 |
| Hydrogen richness/% by weight | 10.9 |
| Sulphur content/% by weight | 0.9 |
| Metal content/μ g.g -1 | 180 |
| Distillate content/% by weight | |
| Initial boiling point | 263 |
| 5％ | 323 |
| 10％ | 361 |
| 30％ | 460 |
| 50％ | 530 |
Table 3
Table 4
| The composition of gas | % by weight |
| Methane | 11.1 |
| Ethane | 2.6 |
| Ethene | 1.8 |
| Propane | 1.5 |
| Propylene | 2.1 |
| C 4+Hydro carbons | 2.4 |
| Hydrogen | 1.6 |
| Carbonic acid gas | 51.2 |
| Carbon monoxide | 25.2 |
| Hydrogen sulfide | 0.2 |
| Nitrogen | 0.3 |
| Amount to | 100 |
Table 5
| The composition of synthetic gas | Volume % |
| Methane | 1.8 |
| Hydrogen | 44.2 |
| Carbon monoxide | 38.8 |
| Carbonic acid gas | 15.2 |
| Amount to | 100 |
Embodiment 2
The present embodiment is for illustrating the combine production method of described coal cracking provided by the invention and heavy oil cracking.
As shown in Figure 1, the coal dust that is the 0.05-1 millimeter by the particle diameter of 100 weight parts (forming as shown in Table 1) is heated to 100 ℃, then add in the coal cracking reactor, and (temperature is 850 ℃ with the 3rd solid product from coal gasification reactor, particle diameter is the 0.05-3 millimeter) mix, the weight ratio that makes coal dust and the 3rd solid product is 1: 6, thereby is 590 ℃ by the temperature regulation of described coal cracking reactor, and pressure is adjusted to 0.2MPa.After processing, the coal cracking reactor obtains gaseous product and solid product, i.e. the first gaseous product and the first solid product.
The heavy crude of 10 weight parts (forming as above shown in table 2) is heated to 300 ℃, then add in the heavy oil cracking reactor, and mix with the first solid product (temperature is 580 ℃) from the coal cracking reactor, making heavy crude in described heavy oil cracking reactor and the weight ratio of described the first solid product is 1: 5, thereby by the temperature regulation of described heavy oil cracking reactor, be 550 ℃, pressure is adjusted to 0.2MPa.Obtain gaseous product and solid product after the heavy oil cracking reactor for treatment, i.e. the second gaseous product and the second solid product.
To add in coal gasification reactor from second solid product (temperature is 525 ℃) of heavy oil breaking reactor, and the mixed gas (temperature is 250 ℃) that injection contains water vapor and oxygen wherein, so that this second solid product generation coal gasification reaction, the weight ratio of described the second solid product, water vapor and oxygen is 3: 5: 1, thereby is 900 ℃ by the temperature regulation in described coal gasification reactor.After processing, coal gasification reactor obtains gasification product and solid product, i.e. third product component and the 3rd solid product.Make the solid product produced in described coal gasification reactor be circulated in described coal cracking reactor simultaneously.
For convenience of operation, described the first gaseous product and described the second gaseous product are converged, and adopt the mode of temperature control condensation to be separated.Table 6 is that coal scission reaction and heavy oil cracking react product and the yield thereof while reaching material balance, and coal gasification reaction produces the yield of synthetic gas, and in table 6 from the product of coal scission reaction and heavy oit pyrolysis reaction shown in the table 7 composed as follows of isolated gas, from the product of coal gasification reaction shown in the table 8 composed as follows of isolated synthetic gas.
Table 6
Table 7
| The composition of gas | % by weight |
| Methane | 12.9 |
| Ethane | 4.6 |
| Ethene | 2.7 |
| Propane | 1.7 |
| Propylene | 4.2 |
| C 4+Hydro carbons | 4.0 |
| Hydrogen | 1.3 |
| Carbonic acid gas | 47.2 |
| Carbon monoxide | 20.8 |
| Hydrogen sulfide | 0.2 |
| Nitrogen | 0.4 |
| Amount to | 100 |
Table 8
| The composition of synthetic gas | Volume % |
| Methane | 2.2 |
| Hydrogen | 46.7 |
| Carbon monoxide | 32.9 |
| Carbonic acid gas | 18.2 |
| Amount to | 100 |
Embodiment 3
The present embodiment is for illustrating the combine production method of described coal cracking provided by the invention and heavy oil cracking.
As shown in Figure 2, the coal dust that is the 0.3-2 millimeter by the particle diameter of 100 weight parts (forming as shown in Table 1) is heated to 250 ℃, then add in the coal cracking reactor, and (temperature is 1100 ℃ with the 3rd solid product from coal gasification reactor, particle diameter is the 0.01-3 millimeter) mix, the weight ratio that makes coal dust and the 3rd solid product is 1: 2, thereby is 550 ℃ by the temperature regulation of described coal cracking reactor, and pressure is adjusted to 0.15MPa.After processing, the coal cracking reactor obtains gaseous product and solid product, i.e. the first gaseous product and the first solid product.
The heavy crude of 10 weight parts (forming as above shown in table 2) is heated to 200 ℃, then add in the heavy oil cracking reactor, and mix with the first solid product (temperature is 535 ℃) from the coal cracking reactor with from the 3rd solid product (temperature is 1100 ℃) of coal gasification reactor, adding described first solid product of heavy oil cracking reactor and the weight ratio of described the 3rd solid product is 1: 0.2, adding the weight ratio of the total amount of heavy crude in the heavy oil cracking reactor and described the first solid product and described the 3rd solid product is 1: 6, thereby it is 500 ℃ by the temperature regulation of described heavy oil cracking reactor, pressure is adjusted to 0.25MPa.Obtain gaseous product and solid product after the heavy oil cracking reactor for treatment, i.e. the second gaseous product and the second solid product.
To add in coal gasification reactor from second solid product (temperature is 480 ℃) of heavy oil breaking reactor, and the mixed gas (temperature is 300 ℃) that injection contains water vapor and oxygen wherein, so that this second solid product generation coal gasification reaction, the weight ratio of described the second solid product, water vapor and oxygen is 2: 6: 1, thereby is 1105 ℃ by the temperature regulation in described coal gasification reactor.After processing, coal gasification reactor obtains gasification product and solid product, i.e. third product component and the 3rd solid product.Make the solid product produced in described coal gasification reactor be circulated in described coal cracking reactor and described heavy oil cracking reactor simultaneously.
For convenience of operation, described the first gaseous product and described the second gaseous product are converged, and adopt the mode of temperature control condensation to be separated.Table 9 is that coal scission reaction and heavy oil cracking react product and the yield thereof while reaching material balance, and coal gasification reaction produces the yield of synthetic gas, and in table 9 from the product of coal scission reaction and heavy oit pyrolysis reaction shown in the table 10 composed as follows of isolated gas, from the product of coal gasification reaction shown in the table 11 composed as follows of isolated synthetic gas.
Table 9
Table 10
| The composition of gas | % by weight |
| Methane | 10.5 |
| Ethane | 2.8 |
| Ethene | 1.9 |
| Propane | 1.7 |
| Propylene | 2.2 |
| C 4+Hydro carbons | 3.7 |
| Hydrogen | 0.9 |
| Carbonic acid gas | 53.6 |
| Carbon monoxide | 21.4 |
| Hydrogen sulfide | 1.0 |
| Nitrogen | 0.3 |
| Amount to | 100 |
Table 11
| The composition of synthetic gas | Volume % |
| Methane | 1.6 |
| Hydrogen | 42.1 |
| Carbon monoxide | 44.1 |
| Carbonic acid gas | 12.2 |
| Amount to | 100 |
Can find out according to above embodiment 1-3, adopt the combine production method of coal cracking provided by the invention and heavy oil cracking to realize the combination producing of coal cracking, heavy oil cracking and gasification.
Claims (14)
1. the combine production method of a coal cracking and heavy oil cracking, is characterized in that, the method comprises the following steps:
(1) under the condition of coal cracking, coal is contacted with the first thermal barrier, obtain the first solid product and the first gaseous product;
(2) under the condition of heavy oil cracking, mink cell focus is contacted with the second thermal barrier, obtain the second solid product and the second gaseous product, the second thermal barrier comprises the first solid product;
(3) under the condition of gasification, the second solid product is contacted with oxygen with water vapor, obtain the 3rd solid product and the 3rd gaseous product; And the first thermal barrier and/or the second thermal barrier comprise the 3rd solid product.
2. method according to claim 1, wherein, described the first thermal barrier is the 3rd solid product, described the second thermal barrier is the first solid product.
3. method according to claim 1, wherein, described the first thermal barrier is the 3rd solid product, the mixture that described the second thermal barrier is the first solid product and the 3rd solid product.
4. method according to claim 3, wherein, in the second thermal barrier, the weight ratio of the first solid product and the 3rd solid product is 1: 0.1-10.
5. according to the described method of any one in claim 1-4, wherein, the condition of described coal cracking comprises that the temperature that coal contacts with the first thermal barrier is 450-700 ℃.
6. method according to claim 5, wherein, the temperature of the first thermal barrier is 800-1200 ℃, and the weight ratio of coal and this first thermal barrier is 1: 1-10.
7. method according to claim 5, wherein, the condition of described coal cracking also comprises that the pressure that coal contacts with the first thermal barrier is 0.1-0.6MPa.
8. according to the described method of any one in claim 1-4, wherein, the particle diameter of described coal is the 0.05-2 millimeter, and the particle diameter of the 3rd solid product is the 0.02-3 millimeter.
9. according to the described method of any one in claim 1-4, wherein, the condition of described heavy oil cracking comprises that the temperature that mink cell focus contacts with the second thermal barrier is 450-650 ℃.
10. method according to claim 9, wherein, in the second thermal barrier, the temperature of the first solid product is 450-700 ℃, and the temperature of the 3rd solid product is 800-1200 ℃, and the weight ratio of described mink cell focus and the second thermal barrier is 1: 4-50.
11. method according to claim 9, wherein, the condition of described heavy oil cracking also comprises that the pressure that mink cell focus contacts with the second thermal barrier is 0.1-0.6MPa.
12. according to the described method of any one in claim 1-4, wherein, the condition of described gasification comprises: the temperature that described the second solid product contacts with oxygen with water vapor is 800-1200 ℃.
13. method according to claim 12, wherein, the temperature of the second solid product is 450-650 ℃, and the weight ratio of the second solid product, water vapor and oxygen is 2-5: 4-10: 1.
14. method according to claim 12, wherein, the condition of described gasification also comprises that the pressure that described the second solid product contacts with oxygen with water vapor is 0.1-0.6MPa.
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| GB779901A (en) * | 1954-08-06 | 1957-07-24 | Erwin Bluemner | Improvements relating to the cracking of coal oil mixtures |
| WO2000061705A1 (en) * | 1999-04-07 | 2000-10-19 | Ensyn Group Inc. | Rapid thermal processing of heavy hydrocarbon feedstocks |
| CN1609169A (en) * | 2003-10-17 | 2005-04-27 | 中国科学院过程工程研究所 | Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system |
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| CN1521234A (en) * | 2003-02-12 | 2004-08-18 | 田原宇 | Cyclic cracking and gasification technology for heavy oil solid heat carrier |
| CN100582197C (en) * | 2006-11-08 | 2010-01-20 | 浙江大学 | Circulating fluidized bed heat-power-gas-tar multi-joint-production apparatus and method |
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|---|---|---|---|---|
| GB779901A (en) * | 1954-08-06 | 1957-07-24 | Erwin Bluemner | Improvements relating to the cracking of coal oil mixtures |
| WO2000061705A1 (en) * | 1999-04-07 | 2000-10-19 | Ensyn Group Inc. | Rapid thermal processing of heavy hydrocarbon feedstocks |
| CN1609169A (en) * | 2003-10-17 | 2005-04-27 | 中国科学院过程工程研究所 | Method of cracking heavy hydrocarbon to prepare low-carbon olefin and the cracking gasifier system |
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| 邹仁鋆.砂子裂解炉.《石油化工裂解原理与技术》.化学工业出版社,1981,第67-74页、第171-174页. * |
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