CN102382667A - Coal cracking and heavy oil cracking joint production method - Google Patents
Coal cracking and heavy oil cracking joint production method Download PDFInfo
- Publication number
- CN102382667A CN102382667A CN2011100745684A CN201110074568A CN102382667A CN 102382667 A CN102382667 A CN 102382667A CN 2011100745684 A CN2011100745684 A CN 2011100745684A CN 201110074568 A CN201110074568 A CN 201110074568A CN 102382667 A CN102382667 A CN 102382667A
- Authority
- CN
- China
- Prior art keywords
- coal
- solid product
- cracking
- thermal barrier
- heavy oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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, poor qualityization day by day, and heavy component carbon residue in some crude oil and metal content are all very high, is difficult to efficiently it fully utilized with traditional processing 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 the important method that is made geseous fuel, synthetic gas and liquid fuel by coal, also have a kind of more economical method in addition: dry distillation of coal method.The whole temperature of destructive distillation is lower than 700 ℃ and is low-temperature pyrolysis, and the whole temperature of destructive distillation is higher than 900 ℃ and is called coking or high temperature carbonization.Low-temperature pyrolysis can obtain tar, coal gas and semicoke.High temperature carbonization mainly obtains coke.Compare with raw coal, the pollutent that semicoke contains is less than raw coal, and is 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 fs gained oil plant, and the coal tar repeated hydrogenation is refining can to get oil fuel, compares with liquefaction, and cost is relatively low.
Rich coal resources in China, raw coal is used for coking, transforms the processing except that part, and the overwhelming majority is used for direct burning.Coal directly burnt, and not only thermo-efficiency is low, serious to environment damage, and the hydrogen-rich component that has higher economic worth in the coal can not get reasonable utilization.Therefore, developing coal conversion is that the technological process of 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 with raw coal combustion, make it under relatively mild condition, extract partially liq fuel and fine chemicals has great importance.For example; Disclosing a kind of among the CN 101016482A is the fine coal grading cleaning multiple utilization technology of the first step with the pyrolysis, comprises raw coal processing and preparing, pyrolysis, burning or gasification, and pyrogenic processes is provided with Coal Chemical Industry isolation of purified system; Wherein, Raw coal fine coal entering pyrogenic processes with certain particle size after processing and preparing is carried out pyrolysis, and the gas-phase product after the pyrolysis gets into 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 the pyrolysis is selected as follows: (1) gets into the burning of burning operation, utilizes heat energy power-generating, heat supply; (2) get into the gasification process gasification, produce synthetic raw gas; (3) get into the burning of burning operation, gasification process gasification simultaneously respectively.
Handling BO technology commonly used at present is delayed coking, and this technology obtains products such as part coker gasoline, coker gas oil, coking distillate, hydrocarbon gas and coke through making the BO thermally splitting.In this technology, because BO needs at high temperature to generate lighter oil product through the long time through thermally splitting, when the raw material carbon residue was very high, the green coke amount was very big.In order to address this problem, developed the heavy oil cracking technology that temperature of reaction is higher, the residence time is short.For example, CN 1504404A discloses a kind of oil refining and gasification process combined method, and wherein, this method may further comprise the steps: (1) petroleum hydrocarbon contacts in reactor drum, reacts with coke transfer agent; (2) separate reaction oil gas that generates and the coke transfer agent that reacts the back 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 behind stripping; (3) in vapourizing furnace, the coke transfer agent of carbon deposit contacts under gasification condition with oxygen-containing gas with water vapor, to generate synthesis gas, makes the coke transfer agent of carbon deposit obtain regeneration simultaneously; (4) coke transfer agent after step (3) regeneration returns in the described reactor drum 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 that produces in said coal cracking and the heavy oil cracking process can not recycle, thereby causes heat recovery efficiency not high.
Summary of the invention
The present invention is in order to overcome the above-mentioned defective that existing coal cleavage method and heavy oil cracking method exist separately; The combine production method of a kind of coal cracking and heavy oil cracking is provided; Adopt this method can realize coal cracking and heavy oil cracking simultaneously; Make the solid product that produces separately in coal cracking and the heavy oil cracking process to recycle simultaneously, thereby saved energy consumption greatly as thermal barrier.
The invention provides the combine production method of a kind of coal cracking and heavy oil cracking, this method comprises: (1) makes coal contact with first thermal barrier under coal cracked condition, obtains first solid product and first gaseous product; (2) under the condition of heavy oil cracking, BO is contacted with second thermal barrier, obtain second solid product and second gaseous product, second thermal barrier comprises first solid product; (3) under the condition of gasification, second solid product is contacted with oxygen with water vapor, obtain the 3rd solid product and the 3rd gaseous product; And first thermal barrier and/or second thermal barrier comprise the 3rd solid product.
The combine production method of coal cracking according to the present invention and heavy oil cracking; Through coal cracking, heavy oil cracking and four processes of gasification are combined; And formation round-robin mass transfer system; The solid product that makes the coal cracking produce can get in the heavy oil cracking reactor drum, as the thermal barrier of heavy oil cracking reaction; And the solid product that heavy oil cracking produces can get into and contacts with oxygen with water vapor in the coal gasification reactor; Thereby generation coal gasification reaction; Since the solid product that heavy oil cracking produces with understand the generation thermopositive reaction after oxygen contact; Making in the coal gasification reactor that fully the solid product of gasification absorbs in this thermopositive reaction does not produce heat, thereby has higher temperature; Through the said solid product that does not fully gasify is circulated in said coal cracking reactor and/or the heavy oil cracking reactor drum, heat to be provided to said coal cracking reactor and/or heavy oil cracking reactor drum.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 that produces in each comfortable coal cracking and the heavy oil cracking process to recycle, thereby saved the energy consumption in the production process greatly as thermal barrier.
Description of drawings
Fig. 1 representes the schema according to the production process of the embodiment of the invention 1 and 2;
Fig. 2 representes the schema according to the production process of the embodiment of the invention 3.
Embodiment
Combine production method according to coal cracking of the present invention and heavy oil cracking may further comprise the steps:
(1) under coal cracked condition, coal is contacted with first thermal barrier, obtain first solid product and first gaseous product;
(2) under the condition of heavy oil cracking, BO is contacted with second thermal barrier, obtain second solid product and second gaseous product, second thermal barrier comprises first solid product;
(3) under the condition of gasification, second solid product is contacted with oxygen with water vapor, obtain the 3rd solid product and the 3rd gaseous product; And first thermal barrier and/or second thermal barrier comprise the 3rd solid product.
In step (1); Coal is under the effect of first thermal barrier, and the temperature of said coal raises and cracking takes place, and discharges most of volatile wherein; Thereby comprising gaseous product and solid product in the split product that obtains, also is first gaseous product and first solid product.Said first solid product mainly comprises semicoke and coke powder, and said semicoke is mainly produced by the coal scission reaction, and said coke powder is mainly from the thermal barrier that gets in said first reactor drum.Said 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 drum of various routines, as long as this reactor drum can be realized the coal scission reaction, therefore, this reactor drum can be called the coal cracking reactor.Said coal cracking reactor for example can be the reactor drum of fluidized-bed reactor, riser reactor, down-flow reactor, moving-burden bed reactor or their array configuration.In the present invention, said first solid product is meant the solid product of from the coal cracking reactor, discharging, and said first gaseous product is meant expellant gas product from the coal cracking reactor.
In step (2); BO is under the effect of second thermal barrier; The temperature of said BO raises rapidly, atomizes, simultaneously the BO generation heat scission reaction after the atomizing; Thereby comprising gaseous product and solid product in the split product that obtains, also is second gaseous product and second solid product.Said second solid product mainly comprises the coke powder particle, and said 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 drum of various routines, as long as this reactor drum can be realized the heavy oil cracking reaction, therefore, this reactor drum can be called the heavy oil cracking reactor drum.Said heavy oil cracking reactor drum for example can be the reactor drum of fluidized-bed reactor, riser reactor, down-flow reactor or their array configuration.In the present invention, said second solid product is meant the solid product of from the heavy oil cracking reactor drum, discharging, and said second gaseous product is meant expellant gas product from the heavy oil cracking reactor drum.
In step (3), under the condition of gasification, contact with oxygen with the generation coal gasification reaction with water vapor through the solid product that the heavy oil cracking reaction is produced, thereby generate solid product and gaseous product, also be the 3rd solid product and the 3rd gaseous product.Said the 3rd solid product mainly contains not the fully coke powder particle of gasification, and said 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 drum of various routines, as long as this reactor drum can be realized coal gasification reaction, therefore; This reactor drum can be called coal gasification reactor, and said coal gasification reactor for example can be fluidized-bed reactor.In the present invention, said the 3rd solid product is meant the solid product of from coal gasification reactor, discharging, and said the 3rd gaseous product is meant expellant gas product from coal gasification reactor.
A preferred embodiment of the invention, said first thermal barrier is the 3rd solid product, said second thermal barrier is first solid product.
According to another kind of preferred implementation of the present invention, said first thermal barrier is the 3rd solid product, and said second thermal barrier is the mixture of first solid product and the 3rd solid product.In this case, the weight ratio of first solid product and the 3rd solid product is 1 in second thermal barrier: 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 BO.
According to method provided by the invention, said coal cracked condition can suitably be selected in the coal crack reacting condition of routine.Under the preferable case, said coal cracked condition comprises that the temperature that coal contacts with first thermal barrier is 450-700 ℃, more preferably 450-650 ℃.In this case, the temperature of 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, said coal cracked condition comprises that also the pressure that coal contacts with first thermal barrier is 0.1-0.6MPa, more preferably 0.1-0.4MPa.In the present invention, said pressure is meant absolute pressure; The temperature that said coal contacts with first thermal barrier is meant the temperature of environment of living in when coal contacts with first thermal barrier, also is coal with after first thermal barrier mixes, and temperature heat passage and when reaching balance takes place for the two.
In a kind of preferred implementation, for making coal cracking more fully, also comprise according to method provided by the invention making coal before contacting, be heated to 100-350 ℃ with first thermal barrier.
In the present invention, said coal can be for having the various coals of conventional particle diameter, and under the preferable case, the particle diameter of said coal is the 0.05-2 millimeter.Said coal for example can be in peat, brown charcoal and the bituminous coal at least a.
According to method provided by the invention, the condition of said heavy oil cracking can suitably be selected in the heavy oil cracking reaction conditions of routine.Under the preferable case, the condition of said heavy oil cracking comprises that the temperature that BO contacts with second thermal barrier is 450-650 ℃, more preferably 450-550 ℃.In this case, in second thermal barrier, the temperature of first solid product is 450-700 ℃, and the temperature of the 4th solid product is 800-1200 ℃, and the weight ratio of the said BO and second thermal barrier is 1: 4-50 is preferably 1: 5-20.Under further preferable case, the condition of said heavy oil cracking comprises that also the pressure that BO contacts with second thermal barrier is 0.1-0.6MPa, more preferably 0.1-0.4MPa.The temperature that said BO contacts with second thermal barrier is meant the temperature of environment of living in when BO contacts with second thermal barrier, also is BO with after second thermal barrier mixes, and temperature heat passage and when reaching balance takes place for the two.
In a kind of preferred implementation, for making BO cracking more fully, also comprise according to method provided by the invention making BO before contacting, be heated to 150-500 ℃ with second thermal barrier, more preferably be heated to 200-450 ℃.
In the present invention, said BO can be the BO of various routines, for example can be in heavy crude, long residuum, normal pressure wax oil, vacuum residuum, wax tailings, jar end oil, deasphalted oil, viscous crude and the hydrocracking tail oil at least a.
According to method provided by the invention, the condition of said gasification can suitably be selected in the gasification condition of routine.Under the preferable case, the condition of said gasification comprises that the temperature that second solid product and water vapor contact with oxygen is 800-1200 ℃, is preferably 800-1000 ℃.In this case, the temperature of second solid product can be 450-650 ℃, and the weight ratio of second solid product, water vapor and oxygen is 2-5: 4-10: 1.Under further preferable case, the condition of said gasification comprises that also the pressure that said material and water vapor contact with oxygen is 0.1-0.6MPa, is preferably 0.1-0.4MPa.
According to method provided by the invention, said water vapor and oxygen can add with the form of the mixed gas that contains water vapor and oxygen, and the temperature of said water vapor and oxygen can be 150-800 ℃, is preferably 300-600 ℃.
Under above-mentioned gasification condition, second solid product is preferably the 0.01-3 millimeter with water vapor contacts the solid product (i.e. the 3rd solid product) of back generation with oxygen particle diameter.
According to one embodiment of the present invention, said method can also comprise separates with said second gaseous product said first gaseous product, to separate into heavy oil fraction, diesel oil distillate, gasoline fraction, water and gas.Said isolating method can adopt conventional method to implement, and for example can adopt the mode of temperature control condensation to separate according to the difference of the condensing temperature of each different components.
In the present invention, can implement separately separately, implement together again after also can the two being converged to separate said first gaseous product and separating of said second gaseous product.Consider production cost, implement together again after preferably the two being converged to separate.
According to one embodiment of the present invention, said method can also comprise discharges said second solid product of part, and the coke powder product of cooling to obtain, and makes said second solid product of other part carry out coal gasification reaction simultaneously.The amount of discharging and carrying out said second solid product of refrigerative can be preferably 20-50 weight % for the 5-60 weight % of the gross weight of said second solid product.
Below through embodiment the present invention is done further detailed explanation.
Embodiment 1
Present embodiment is used to explain the combine production method of said coal cracking provided by the invention and heavy oil cracking.
As shown in Figure 1; With the particle diameter of 100 weight parts is that the coal dust (forming as shown in table 1 below) of 0.3-2 millimeter is heated to 200 ℃, add then 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 ℃ with the temperature regulation of said coal cracking reactor, and pressure is adjusted to 0.3MPa.After handling, process coal cracking reactor obtains gaseous product and solid product, i.e. first gaseous product and first solid product.
The heavy crude (forming as shown in table 2 below) of 10 weight parts is heated to 200 ℃; Add then in the heavy oil cracking reactor drum; And with mix from first solid product in the coal cracking reactor (temperature is 550 ℃); Making heavy crude and the weight ratio of said first solid product in the said heavy oil cracking reactor drum is 1: 8, thereby is 500 ℃ with the temperature regulation of said heavy oil cracking reactor drum, and pressure is adjusted to 0.3MPa.Obtain gaseous product and solid product after the process heavy oil cracking reactor for treatment, i.e. second gaseous product and second solid product.
To add from second solid product (temperature is 480 ℃) of heavy oil breaking reactor drum in the coal gasification reactor; And to wherein injecting the mixed gas (temperature is 200 ℃) that contains water vapor and oxygen; So that this second solid product generation coal gasification reaction; The weight ratio of said second solid product, water vapor and oxygen is 3: 6: 1, thereby is 1000 ℃ with the temperature regulation in the said coal gasification reactor.After handling, the process coal gasification reactor obtains gasification product and solid product, i.e. third product component and the 3rd solid product.The solid product that produces in the said coal gasification reactor is circulated in the said coal cracking reactor.
Be handled easily, said first gaseous product and said second gaseous product are converged, and adopt the mode of temperature control condensation to separate.Table 3 is that coal scission reaction and heavy oil cracking react product and yield thereof when reaching material balance; And coal gasification reaction produces the yield of synthetic gas; And in the table 3 from the product of coal scission reaction and heavy oit pyrolysis reaction the composition of isolated gas as shown in table 4 below, the composition of isolated synthetic gas is as shown in table 5 below from the product of coal gasification reaction.
Table 1
Table 2
| Project | |
| Density (20 ℃)/g.cm -3 | 1.07 |
| Kinematic viscosity (80 ℃)/mm 2·s -1 | 3648 |
| Carbon residue/weight % | 13.9 |
| Carbon content/weight % | 86.5 |
| Hydrogen richness/weight % | 10.9 |
| Sulphur content/weight % | 0.9 |
| Metal content/μ g.g -1 | 180 |
| Distillate content/weight % | |
| Over point | 263 |
| 5％ | 323 |
| 10％ | 361 |
| 30％ | 460 |
| 50％ | 530 |
Table 3
Table 4
| The composition of gas | 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
Present embodiment is used to explain the combine production method of said coal cracking provided by the invention and heavy oil cracking.
As shown in Figure 1; With the particle diameter of 100 weight parts is that the coal dust (forming as above shown in the table 1) of 0.05-1 millimeter is heated to 100 ℃, add then 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 ℃ with the temperature regulation of said coal cracking reactor, and pressure is adjusted to 0.2MPa.After handling, process coal cracking reactor obtains gaseous product and solid product, i.e. first gaseous product and first solid product.
The heavy crude (forming as above shown in the table 2) of 10 weight parts is heated to 300 ℃; Add then in the heavy oil cracking reactor drum; And with mix from first solid product in the coal cracking reactor (temperature is 580 ℃); Making heavy crude and the weight ratio of said first solid product in the said heavy oil cracking reactor drum is 1: 5, thereby is 550 ℃ with the temperature regulation of said heavy oil cracking reactor drum, and pressure is adjusted to 0.2MPa.Obtain gaseous product and solid product after the process heavy oil cracking reactor for treatment, i.e. second gaseous product and second solid product.
To add from second solid product (temperature is 525 ℃) of heavy oil breaking reactor drum in the coal gasification reactor; And to wherein injecting the mixed gas (temperature is 250 ℃) that contains water vapor and oxygen; So that this second solid product generation coal gasification reaction; The weight ratio of said second solid product, water vapor and oxygen is 3: 5: 1, thereby is 900 ℃ with the temperature regulation in the said coal gasification reactor.After handling, the process coal gasification reactor obtains gasification product and solid product, i.e. third product component and the 3rd solid product.The solid product that produces in the said coal gasification reactor is circulated in the said coal cracking reactor.
Be handled easily, said first gaseous product and said second gaseous product are converged, and adopt the mode of temperature control condensation to separate.Table 6 is that coal scission reaction and heavy oil cracking react product and yield thereof when reaching material balance; And coal gasification reaction produces the yield of synthetic gas; And in the table 6 from the product of coal scission reaction and heavy oit pyrolysis reaction the composition of isolated gas as shown in table 7 below, the composition of isolated synthetic gas is as shown in table 8 below from the product of coal gasification reaction.
Table 6
Table 7
| The composition of gas | 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
Present embodiment is used to explain the combine production method of said coal cracking provided by the invention and heavy oil cracking.
As shown in Figure 2; With the particle diameter of 100 weight parts is that the coal dust (forming as above shown in the table 1) of 0.3-2 millimeter is heated to 250 ℃, add then 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 ℃ with the temperature regulation of said coal cracking reactor, and pressure is adjusted to 0.15MPa.After handling, process coal cracking reactor obtains gaseous product and solid product, i.e. first gaseous product and first solid product.
The heavy crude (forming as above shown in the table 2) of 10 weight parts is heated to 200 ℃; Add then in the heavy oil cracking reactor drum; And with mix from first solid product in the coal cracking reactor (temperature is 535 ℃) with from the 3rd solid product (temperature is 1100 ℃) of coal gasification reactor; Adding said first solid product of heavy oil cracking reactor drum and the weight ratio of said the 3rd solid product is 1: 0.2; The weight ratio of the heavy crude in the adding heavy oil cracking reactor drum and the total amount of said first solid product and said the 3rd solid product is 1: 6; Thereby with the temperature regulation of said heavy oil cracking reactor drum is 500 ℃, and pressure is adjusted to 0.25MPa.Obtain gaseous product and solid product after the process heavy oil cracking reactor for treatment, i.e. second gaseous product and second solid product.
To add from second solid product (temperature is 480 ℃) of heavy oil breaking reactor drum in the coal gasification reactor; And to wherein injecting the mixed gas (temperature is 300 ℃) that contains water vapor and oxygen; So that this second solid product generation coal gasification reaction; The weight ratio of said second solid product, water vapor and oxygen is 2: 6: 1, thereby is 1105 ℃ with the temperature regulation in the said coal gasification reactor.After handling, the process coal gasification reactor obtains gasification product and solid product, i.e. third product component and the 3rd solid product.The solid product that produces in the said coal gasification reactor is circulated in said coal cracking reactor and the said heavy oil cracking reactor drum.
Be handled easily, said first gaseous product and said second gaseous product are converged, and adopt the mode of temperature control condensation to separate.Table 9 is that coal scission reaction and heavy oil cracking react product and yield thereof when reaching material balance; And coal gasification reaction produces the yield of synthetic gas; And in the table 9 from the product of coal scission reaction and heavy oit pyrolysis reaction the composition of isolated gas as shown in table 10 below, the composition of isolated synthetic gas is as shown in table 11 below from the product of coal gasification reaction.
Table 9
Table 10
| The composition of gas | 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 coal cracking and heavy oil cracking is characterized in that this method may further comprise the steps:
(1) under coal cracked condition, coal is contacted with first thermal barrier, obtain first solid product and first gaseous product;
(2) under the condition of heavy oil cracking, BO is contacted with second thermal barrier, obtain second solid product and second gaseous product, second thermal barrier comprises first solid product;
(3) under the condition of gasification, second solid product is contacted with oxygen with water vapor, obtain the 3rd solid product and the 3rd gaseous product; And first thermal barrier and/or second thermal barrier comprise the 3rd solid product.
2. method according to claim 1, wherein, said first thermal barrier is the 3rd solid product, said second thermal barrier is first solid product.
3. method according to claim 1, wherein, said first thermal barrier is the 3rd solid product, said second thermal barrier is the mixture of first solid product and the 3rd solid product.
4. method according to claim 3, wherein, the weight ratio of first solid product and the 3rd solid product is 1 in second thermal barrier: 0.1-10.
5. according to any described method among the claim 1-4, wherein, said coal cracked condition comprises that the temperature that coal contacts with first thermal barrier is 450-700 ℃.
6. method according to claim 5, wherein, the temperature of 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, said coal cracked condition comprises that also the pressure that coal contacts with first thermal barrier is 0.1-0.6MPa.
8. according to any described method among the claim 1-4, wherein, the particle diameter of said 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 any described method among the claim 1-4, wherein, the condition of said heavy oil cracking comprises that the temperature that BO contacts with second thermal barrier is 450-650 ℃.
10. method according to claim 9, wherein, in second thermal barrier, the temperature of first solid product is 450-700 ℃, and the temperature of the 3rd solid product is 800-1200 ℃, and the weight ratio of the said BO and second thermal barrier is 1: 4-50.
11. method according to claim 9, wherein, the condition of said heavy oil cracking comprises that also the pressure that BO contacts with second thermal barrier is 0.1-0.6MPa.
12. according to any described method among the claim 1-4, wherein, the condition of said gasification comprises: said second solid product is 800-1200 ℃ with the temperature that water vapor contacts with oxygen.
13. method according to claim 12, wherein, the temperature of second solid product is 450-650 ℃, and the weight ratio of second solid product, water vapor and oxygen is 2-5: 4-10: 1.
14. method according to claim 12, wherein, the condition of said gasification comprises that also the pressure that said second solid product and water vapor contact with oxygen is 0.1-0.6MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110074568 CN102382667B (en) | 2010-09-01 | 2011-03-24 | Coal cracking and heavy oil cracking joint production method |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010270294 | 2010-09-01 | ||
| CN201010270294.1 | 2010-09-01 | ||
| CN 201110074568 CN102382667B (en) | 2010-09-01 | 2011-03-24 | Coal cracking and heavy oil cracking joint production method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102382667A true CN102382667A (en) | 2012-03-21 |
| CN102382667B CN102382667B (en) | 2013-12-25 |
Family
ID=45822508
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110074568 Active CN102382667B (en) | 2010-09-01 | 2011-03-24 | Coal cracking and heavy oil cracking joint production method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102382667B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110903848A (en) * | 2019-12-17 | 2020-03-24 | 陕西延长石油（集团）有限责任公司 | Device and method for co-converting heavy inferior oil and coal |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN1521234A (en) * | 2003-02-12 | 2004-08-18 | 田原宇 | Cyclic cracking and gasification technology for heavy oil solid heat carrier |
| 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 |
| CN1978591A (en) * | 2006-11-08 | 2007-06-13 | 浙江大学 | Circulating fluidized bed heat-power-gas-tar multi-joint-production apparatus and method |
-
2011
- 2011-03-24 CN CN 201110074568 patent/CN102382667B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN1521234A (en) * | 2003-02-12 | 2004-08-18 | 田原宇 | Cyclic cracking and gasification technology for heavy oil solid heat carrier |
| 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 |
| CN1978591A (en) * | 2006-11-08 | 2007-06-13 | 浙江大学 | Circulating fluidized bed heat-power-gas-tar multi-joint-production apparatus and method |
Non-Patent Citations (1)
| Title |
|---|
| 邹仁鋆: "《石油化工裂解原理与技术》", 31 December 1981, article "砂子裂解炉", pages: 67-74 - 171-174 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110903848A (en) * | 2019-12-17 | 2020-03-24 | 陕西延长石油（集团）有限责任公司 | Device and method for co-converting heavy inferior oil and coal |
| CN110903848B (en) * | 2019-12-17 | 2021-06-04 | 陕西延长石油（集团）有限责任公司 | Device and method for co-converting heavy inferior oil and coal |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102382667B (en) | 2013-12-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8784650B2 (en) | Method and equipment for multistage liquefying of carbonaceous solid fuel | |
| CN101580728B (en) | Process technology for non-caking coal or weak caking coal | |
| US10752850B2 (en) | Combined hydrogenation process method for producing high-quality fuel by medium-low-temperature coal tar | |
| CN102453510B (en) | Combined processing method of copyrolysis of heavy oil and coal | |
| CN101429456B (en) | Delay coking hydrogenation combined process for coal oil | |
| CN105567321A (en) | Method for producing oil product by corefining coal and oil | |
| CN101538473B (en) | Incoherence or weak caking coal deep processing method | |
| CN103788968B (en) | The combination process of a kind of coal and refining of petroleum byproduct copyrolysis | |
| CN102453515A (en) | Inferior heavy oil contact cracking-gasification-regeneration combined method | |
| CN102031154B (en) | Method for comprehensively utilizing lignite | |
| CN103992823A (en) | Method and system for synthesizing methane, gasoline and diesel oil by using low-rank coal and biomass as raw materials | |
| US10526202B2 (en) | Process for production of high quality syngas through regeneration of coked upgradation agent | |
| CN102453511B (en) | Method for preparing synthesis gas by coupled processing of coal and heavy oil | |
| CN104046372A (en) | Method for preparing bio-oil and synthesis gas from biomass | |
| CN102382667B (en) | Coal cracking and heavy oil cracking joint production method | |
| CN102453512B (en) | Processing method for heavy oil and coal copyrolysis | |
| CN104327871B (en) | A kind of moulded coal raw material suitable for tamping coke furnace low-order coal upgrading | |
| CN104046373A (en) | Method for preparing bio-oil and synthesis gas from biomass | |
| CN102382668B (en) | Coal cracking and heavy oil cracking joint production method | |
| CN102382669B (en) | Coal cracking and heavy oil cracking joint production method | |
| CN106433779A (en) | System and method for maximum production of light fuel by coal tar | |
| CN102337144A (en) | Method for preparing light fuel from medium and low-temperature coal tar generated by carbonizing lump coal | |
| CN105400531B (en) | A kind of technique that upgrading is carried out to the coal raw material containing low-order coal using tamping coke furnace | |
| CN109233890A (en) | A kind of oil gas coproduction gasification process and device | |
| CN112538379B (en) | Processing method and device for heavy oil lightening-coproduction synthesis gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |