Patent Application
20170081601
The application claims the priority of Chinese Patent Application No. 201410150177.X, filed on Apr. 15, 2014 and titled “Method for Co-gasification of Coal”, the disclosure of which is incorporated herein in its entirety by reference.
The present invention relates to the field of coal gasification, and in particular to a method for co-gasification of coal.
Coal gasification is a process in which, at a certain temperature and pressure, organic matter in the coal is caused to chemically react with a gasification agent (for example, oxygen) so that solid coal is converted into a combustible gas containing CO, H2, CH4, etc. and an incombustible gas containing CO2, N2, etc. Common coal gasification technologies at present mainly include: coal water slurry gasification technology, pulverized coal gasification technology, biomass gasification technology, and gasification technology for multiple slurries currently in progress of technological improvement. Wherein, methods for gasification of raw gasification material in different phases are obviously different. With regard to co-gasification of raw material of different phases, for example, co-gasification of pulverized coal and coal water slurry, the gasification method is even more complicated and includes specific steps obviously different from those for gasification of coal water slurry only, gasification of pulverized coal only and gasification of multiple slurries only.
CN101760244A disclosed a three-phase multi-material pressurized coal gasification device and a process thereof. The gasification process includes: broken feed coal, water and annexing agent are grinded into coal water slurry, and the coal water slurry enters a combustion chamber from a mixing nozzle; the broken dry pulverized coal is transported by a high-pressure carbon dioxide gas to enter the combustion chamber from the mixing nozzle; and then high-pressure pressurized oxygen is injected into the combustion chamber. At a high temperature, the high-pressure pressurized oxygen chemically reacts with the coal water slurry and the pulverized coal to generate a synthesis gas (an industrial coal gas) mainly composed of carbon oxide and hydrogen. With regard to this method in which raw material of multiple phases is added into a gasifier simultaneously for mixed combustion, instability is prone to occur during the combustion. As a result, components of the synthesis gas might be unstable, or the synthesis gas is relatively low in quality. When the instability mentioned above occurs, an attempt to adjust a plurality of kinds of raw material one by one is required to obtain a relatively stable co-gasification, the adjustment being complicated, time-consuming and highly difficult.
With regard to problems existing in related technologies, an objective of the present invention is to provide a method for co-gasification of coal with stable operation.
For this purpose, the present invention provides a method for co-gasification of coal, including the following steps: step 1: injecting fuel and a first pressurized oxygen-containing gas into a gasifier, and igniting the fuel for a temperature rise inside the gasifier; step 2: when the temperature rise reaches an extent at which pulverized coal to be injected can be ignited, stop injecting the fuel, and maintaining injection of the first pressurized oxygen-containing gas; and injecting a pressurized carbon dioxide gas carrying pulverized coal to be injected into the gasifier for gasification of pulverized coal; step 3: when the gasification of the pulverized coal is stable, injecting coal water slurry and a second pressurized oxygen-containing gas into the gasifier for co-gasification.
With regard to the same pressurized oxygen-containing gas, when the “time to start injection” is different, the gas is differentiated by “the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas”. In other words, the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas are the same pressurized oxygen-containing gas. The words “first and second” are merely used to define that the two pressurized oxygen-containing gases have different “time to start injection”, instead of defining the pressure or the respective parameter composition thereof. Injection positions of the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas can be the same or different.
According to the present invention, in the step 2, an oxygen-coal ratio of the injected first pressurized oxygen-containing gas to the pulverized coal to be injected is within a range from 0.49 Nm3/kg to 0.65 Nm3/kg.
According to the present invention, in the step 3, an oxygen-coal ratio of the injected second pressurized oxygen-containing gas to the coal water slurry is within a range from 0.54 Nm3/kg to 0.70 Nm3/kg.
The oxygen-coal ratio is a ratio of the volume of oxygen to the mass of coal passing an effective cross-section in unit time, i.e., a ratio of a volume flow of oxygen to a mass flow of coal, the unit being: Nm3/kg. The coal is pulverized coal carried by the pressurized carbon dioxide gas and coal in coal water slurry. The mass of the coal is the mass of the pulverized coal carried by the pressurized carbon dioxide gas or the mass of coal in coal water slurry regardless of the mass of gas or water and an annexing agent.
According to the present invention, in the step 3, the coal water slurry and the second pressurized oxygen-containing gas are injected by a first burner provided on a side wall of the gasifier, wherein the mass flow of coal water slurry is greater than or equal to 70% of the load of a first burner.
According to the present invention, the step 3 also includes the following steps: controlling, by adjusting the oxygen-coal ratio of the first pressurized oxygen-containing gas to the pulverized coal to be injected within a range from 0.49 Nm3/kg to 0.65 Nm3/kg and/or adjusting the oxygen-coal ratio of the second pressurized oxygen-containing gas to the coal water slurry within a range from 0.54 Nm3/kg to 0.70 Nm3/kg, an operating temperature of the gasifier.
According to the present invention, in the gasifier with water wall, the operating temperature of the gasifier is controlled within a range from 1400° C. to 1600° C.; and in the firebrick gasifier, the operating temperature of the gasifier is controlled within a range from 1300° C. to 1400° C.
According to the present invention, the step 3 also includes the following steps: controlling, by increasing or decreasing a volume flow of oxygen in the first pressurized oxygen-containing gas, a mass flow of the pulverized coal to be injected, a volume flow of oxygen in the second pressurized oxygen-containing gas and a mass flow of coal in the coal water slurry in an equal proportion, an operating pressure of the gasifier.
According to the present invention, in the gasifier with water wall, the operating pressure of the gasifier is controlled within a range from 4.5 MPa to 7.0 MPa; and in the firebrick gasifier, the operating pressure of the gasifier is controlled within a range from 4.5 MPa to 7.0 MPa.
According to the present invention, in the step 1, by adjusting injection flows of the fuel and the first pressurized oxygen-containing gas, speed of the temperature rise is controlled to be lower than or equal to 50° C./h.
According to the present invention, a temperature at which the pulverized coal to be injected can be ignited is greater than or equal to 400° C.
According to the present invention, in the step 1, the first pressurized oxygen-containing gas and the fuel are injected into the gasifier respectively by isolated passages of a second burner provided on the top of the gasifier; and in the step 2, the pressurized carbon dioxide gas carrying pulverized coal and the first pressurized oxygen-containing gas are injected into the gasifier respectively by isolated passages of the second burner.
According to the present invention, when gasification of the pulverized coal of the step 2 is performed, a black water circulation system of the gasifier is started.
According to the present invention, when the fuel is fuel oil or fuel gas, the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas are both pressurized oxygen, wherein when the fuel is fuel oil, the fuel oil, after being atomized, is injected into the gasifier.
When compared with the existing technologies, the present invention has the following advantageous effects.
With regard to the method for co-gasification of coal of the present invention, first, fuel and the first pressurized oxygen-containing gas are injected into the gasifier and the fuel is ignited for a temperature rise inside the gasifier. Then, when the temperature rise reaches an extent at which pulverized coal to be injected can be ignited, the injection of the fuel is stopped, and the injection of the first pressurized oxygen-containing gas is maintained; and pressurized carbon dioxide gas carrying the pulverized coal to be injected is injected into the gasifier for gasification of pulverized coal. That is, the pulverized coal in the gasifier reacts with the oxygen in the first pressurized oxygen-containing gas to generate a synthesis gas. After the gasification of pulverized coal is stable, coal water slurry and the second pressurized oxygen-containing gas are injected into the gasifier for co-gasification. That is, now, gasification of pulverized coal and gasification of coal water slurry are performed in the gasifier. Thus, co-gasification of coal is formed. By the method for co-gasification of coal, co-gasification is established after ensuring that gasification of pulverized coal is stable, thus ensuring a stable operation during co-gasification, without adjustment steps in the prior art which are complicated, time-consuming and highly difficult.
The specific implementations of the present invention will be described with reference to the accompanying drawings.
With reference to
With reference to
By the method for co-gasification of coal, stable gasification of pulverized coal is established in the gasifier and then co-gasification is performed, thus ensuring a stable operation of the gasifier during co-gasification, without adjustment steps in the prior art which are complicated, time-consuming and highly difficult.
With further reference to
A second burner 2 is provided on the top of the gasifier, and the first pressurized oxygen-gas and the fuel are simultaneously injected by the second burner 2. In addition, the first pressurized oxygen-containing gas and the fuel are injected into the gasifier respectively by isolated passages of the second burner. That is, the first pressurized oxygen-containing gas and the fuel, before being injected, are not mixed. Ignited by an electric spark or naked fire, the fuel is ignited and combusted in the gasifier to cause temperature rise in the gasifier. In this embodiment, the first pressurized oxygen-containing gas is pressurized oxygen, and the pressure of the pressurized oxygen is within a range from 6.5 MPa to 7.5 MPa; and the fuel is liquefied petroleum gas. Of course, the first pressurized oxygen-containing gas may be other pressurized gases containing oxygen, for example, a pressurized gas mixed by vapor and oxygen or a pressurized gas mixed by carbon dioxide gas and oxygen, wherein, “pressurized” means being greater than the pressure of a corresponding gas in an ordinary pressure state. The fuel may be fuel oil or fuel gas well-known to those skilled in the art. In addition, the fuel oil enters the gasifier via the second burner 2 after being atomized therein.
In addition, during the temperature rise in the step 1, by adjusting injection flows of the fuel and the first pressurized oxygen-containing gas, speed of the temperature rise is controlled to be lower than or equal to 50° C./h. It can be understood that when the speed of the temperature rise is greater than 50° C./h, injection flows of the fuel and the first pressurized oxygen-containing gas are reduced to reduce the fuel com busted in the gasifier in unit time. In this way, heat release of the fuel burning in unit time is reduced, and further, the speed of the temperature rise in the gasifier is slowed down. Wherein, the injection flows of the first pressurized oxygen-containing gas and the fuel are optionally respective volume flows when the first pressurized oxygen-containing gas and the fuel are injected. Of course, according to difference in fuel used in actual production, a mass flow or a volume flow can be selected for operation.
In addition, during the temperature rise for the gasifier, smoke generated when the fuel is combusted in the gasifier is exhausted to a flare system via the third pipeline 7. Wherein, the flare system used in the present invention is a flare system well-known to those skilled in the art. The flare system is an important facility for safety and environment protection for a chemical plant, and is mainly used to process combustible gas which cannot be recycled when a production device is in an ON and OFF state and when in a non-normal production state and an emergency state.
In this embodiment, the step 2 is specifically implemented as follows.
When the temperature rise of the gasifier reaches an extent at which the pulverized coal to be injected can be ignited (in this embodiment, the temperature at which the pulverized coal can be ignited is greater than or equal to 400° C.), injection of the fuel by the second burner 2 is stopped, and meanwhile continuous injection of the first pressurized oxygen-containing gas by the second burner 2 is maintained; and the pressurized carbon dioxide gas carrying pulverized coal to be injected is injected into the gasifier by the second burner 2. That is, the fuel injected by the second burner 2 is replaced with the pressurized carbon dioxide gas carrying pulverized coal to be injected. It can be understood by those skilled in the art that, according to the property of the pulverized coal used, the temperature at which the pulverized coal can be ignited can be determined within a temperature range greater than or equal to 400° C. It can also be understood that the purpose of a temperature rise in the gasifier is to increase the temperature inside the gasifier to a temperature at which the pulverized coal to be injected can be combusted, i.e., to an extent at which the pulverized coal can be combusted without increasing the temperature to an extremely high extent. Wherein, the pressure of the pressurized carbon dioxide gas is greater than 6 MPa. In addition, the pulverized coal which is to be injected into the gasifier is regarded as pulverized coal to be injected. If the “pulverized coal” mentioned in the present invention has not been injected into the gasifier and will be injected into the gasifier in the following steps, the “pulverized coal” mentioned is “pulverized coal to be injected”.
Further, when the fuel mentioned above is replaced with the pressurized carbon dioxide gas carrying pulverized coal to be injected, the oxygen-coal ratio of the injected first pressurized oxygen-containing gas to the pulverized coal to be injected is within a range from 0.49 Nm3/kg to 0.65 Nm3/kg. That is, a ratio of the volume flow (volume unit: Nm3) of the oxygen in the injected first pressurized oxygen-containing gas to the mass flow (mass unit: kg) of the pulverized coal to be injected which is injected simultaneously is within a range from 0.49 Nm3/kg to 0.65 Nm3/kg. In this embodiment, the first pressurized oxygen-containing gas is pressurized oxygen. Thus, the volume flow of the oxygen in the first pressurized oxygen-containing gas is the volume flow of the pressurized oxygen. Of course, in other optional embodiments, for example, when the first pressurized oxygen-containing gas is a pressurized gas mixed by vapor and pure oxygen, the volume flow of the oxygen in the first pressurized oxygen-containing gas is the volume flow of the oxygen in the pressurized mixed gas.
By the steps of the step 2, a pulverized coal gasification reaction of the pulverized coal takes place inside the gasifier. Optionally, when the gasification reaction of the pulverized coal starts to take place inside the gasifier, a black water circulation system is started. Specifically, during the gasification of pulverized coal in the first chamber 8, gasified coal ash enters the second chamber 9. Water is transported from the fourth pipeline 10 to the interior of the second chamber 9. The water transported to the interior of the second chamber 9 is mixed with coal ash (that is, “black water” is formed), and the water containing coal ash is discharged by the fifth pipeline 11. In this way, coal ash in the second chamber 9 is discharged. When the water containing coal ash discharged from the fifth pipeline 11 passes through the black water circulation system, the coal ash is removed by filtration and the water is reused. In addition, during the gasification of pulverized coal, the generated synthesis gas is exhausted via the third pipeline 7. In addition, it is detected whether the exhausted synthesis gas is qualified. If the exhausted synthesis gas is qualified, the synthesis gas is transported to a purification procedure downstream; and if the exhausted synthesis gas is not qualified, the synthesis gas is guided to the flare system. For example, with the difference in pressure between the interior of the gasifier and the exterior of the gasifier, the synthesis gas is pumped out. Of course, according to different requirements on actual production, there may be slight difference in standards for deciding whether the exhausted synthesis gas is qualified. Those skilled in the art can detect and decide whether the synthesis gas is qualified according to requirements on actual production.
Optionally, during the gasification of pulverized coal, by adjusting the oxygen-coal ratio of the first pressurized oxygen-containing gas to the pulverized coal to be injected within a range from 0.49 Nm3/kg to 0.65 Nm3/kg, components of the synthesis gas generated by gasification of coal and an operating temperature inside the gasifier are adjusted. Meanwhile, in a case where the oxygen-coal ratio is maintained to be constant, by adjusting the volume flow of the oxygen in the first pressurized oxygen-containing gas and the mass flow of the pulverized coal to be injected, the operating pressure inside the gasifier is adjusted, so that gasification of pulverized coal is becoming stable. Wherein, the method for adjusting the volume flow of the oxygen in the first pressurized oxygen-containing gas and the mass flow of the pulverized coal to be injected will be described in detail below.
In addition, during the actual production, a standard for deciding whether the gasification of coal is stable varies according to different requirements on actual production. Those skilled in the art can decide whether gasification of the pulverized coal is stable or not according to requirements on actual production. For example, components of the synthesis gas exhausted from the third pipeline 7 are detected. If the effective components (CO, H2, CH4) of the synthesis gas are stable, or if the content of one (CO or H2) or some components (CO and H2) meets the requirement, the gasification of pulverized coal is stable. Optionally, when the total volume content by percentage of hydrogen, carbon oxide and methane in the synthesis gas (i.e., percentage of the total volume of the three components to the volume of the generated synthesis gas) varies within the range from 75% to 95%, or when the fluctuation range of the volume content by percentage of hydrogen, carbon oxide or methane in the synthesis gas (i.e., the percentage of the three components respectively to the volume of the synthesis gas) is less than 20%, the effective components (CO, H2, CH4) of the synthesis gas are stable. That is, the gasification of the pulverized gas is stable. In addition, optionally, if the volume content of H2 (i.e., percentage of the volume of H2 to the volume of the synthesis gas) is greater than or equal to 20%, and/or if the volume content of CO (i.e., percentage of the volume of CO to the volume of the synthesis gas) is greater than or equal to 50%, the content of one component (CO or H2) or some components (CO and H2) in the synthesis gas meets the requirement. That is, gasification of the pulverized coal is stable. Of course, the foregoing description is merely an embodiment, numerical values therein can be set according to specific requirements on production, and the present invention is not limited thereto.
In addition, in this embodiment, preferably, a structure of the second burner 2 is a combined multi-nozzle combustor for combustible powder. The combustor includes: an ignition burner located in the center and a plurality of process burners uniformly provided along a peripheral direction at an outer periphery of the ignition burner.
Wherein, the ignition burner includes: a fuel gas passage located in the center of the ignition burner, an ignition device (an ignition match) provided at the front end of the fuel gas passage, and an annular first oxygen passage provided on the outer side of the fuel gas passage. Further, a first cooling jacket is provided between the fuel gas passage and the oxygen passage, and a second cooling jacket is provided outside the oxygen passage. The first pressurized oxygen-containing gas injection pipe 3 is communicated with the first oxygen passage. In this way, the first pressurized oxygen-containing gas is injected into the gasifier via the first pressurized oxygen-containing gas injection pipe 3 and the first oxygen passage, and the fuel is injected into the gasifier via the fuel gas passage, so that the first pressurized oxygen-containing gas and the fuel are injected into the gasifier respectively by the isolated passages of the second burner.
Wherein, each process burner includes: a pulverized coal passage located in the center of the process burner, and an annular second oxygen passage provided on the outer side of the pulverized coal passage. A third cooling jacket is provided outside the second oxygen passage. The first pressurized oxygen-containing gas injection pipe 3 is communicated with the second oxygen passage. The first pipeline 4 is communicated with the pulverized coal passage. In the step 2, the first pressurized oxygen-containing gas is injected into the gasifier via the first pressurized oxygen-containing gas injection pipe 3 and the second oxygen passage, and the pressurized carbon dioxide gas carrying the pulverized coal to be injected is injected into the gasifier via the first pipeline 4 and the pulverized coal passage. In this way, the pressurized carbon dioxide gas carrying the pulverized coal and the first pressurized oxygen-containing gas are injected into the gasifier respectively by the isolated passages of the second burner.
The first cooling jacket, the second cooling jacket and the third cooling jacket form double-layer structure, including an inner layer and an outer layer; and a cooling medium enters from the inner layer and is discharged from the outer layer. The ignition device is preferably movable and can be removed after the pulverized coal is ignited. Pulverized coal, after being ignited, can be delivered into the fuel gas passage. That is, the fuel gas passage can be used as the pulverized coal passage. When the second burner with the structure mentioned above is applied, and when the injection of fuel is stopped, the injection of the first pressurized oxygen-containing gas via the first oxygen passage is changed to via the second oxygen passage. Of course, in other optional embodiments in which the first oxygen passage and the second oxygen passage are the same passage, the change is not performed. In addition, it can be understood that the “maintaining injection of the first pressurized oxygen-containing gas” in the step 2 of the present invention can refer to maintaining an uninterrupted injection of the first pressurized oxygen-containing gas into the gasifier in terms of time, or maintaining an injection of the first pressurized oxygen-containing gas with short intervals as long as the operating temperature of the gasifier reaches an ignition point of pulverized coal and there is adequate oxygen to combust the pulverized coal when the pressurized carbon dioxide gas carrying pulverized coal to be injected is injected into the gasifier. In other embodiments in which the fuel gas passage and the pulverized coal passage are the same passage, both the fuel and the pressurized carbon dioxide gas carrying the pulverized coal are injected via the first pipeline 4 and this same passage.
In addition, the foregoing structure can refer to the structure disclosed in CN101446413A of the prior art, but is not limited thereto. Of course, the second burner 2 can also be the ignition burner or the process burner only.
In addition, the second burner and the furnace body of the gasifier are fixed by a flange.
In this embodiment, the step 3 is specifically implemented as follows.
After the gasification of the pulverized coal is stable, the second pressurized oxygen-containing gas and the coal water slurry are injected by the first burner 1. Specifically, the first burner 1 is arranged on a side wall of the gasifier. Optionally, the first burner 1 is structurally formed of a series of nozzles on concentric tubes. An inner nozzle thereof is a central oxygen flow passage. An annulus passage formed by the outer wall of the inner nozzle and the inner wall of an intermediate nozzle is a flow passage for coal water slurry. An end of the inner nozzle and an end of the intermediate nozzle are separated by a certain distance to form a premixing chamber so that oxygen and coal water slurry can be mixed therein. An annulus passage formed by the outer wall of the intermediate nozzle and the inner wall of the outer nozzle is an outer oxygen flow passage. An end of the intermediate nozzle and an end of the outer nozzle are substantially flush with each other. There is a water cooling coil on the outer surface of the outer nozzle to lower the temperature of the whole burner. The second pressurized oxygen-containing gas injection pipe 5 is communicated with the central oxygen flow passage and the outer oxygen flow passage. The second pipeline 6 is communicated with the coal water slurry flow passage. The coal water slurry is injected into the coal water slurry flow passage through the second pipeline 6. The foregoing structure can refer to the structure disclosed in CN103013574A of the prior art, but is not limited thereto. In other optional embodiments, there may be only one passage for injecting the second pressurized oxygen-containing gas and one passage for injecting the coal water slurry. In addition, the first burner and the furnace body of the gasifier are fixed by a flange.
In this embodiment, the second pressurized oxygen-containing gas and the first pressurized oxygen-containing gas are the same pressurized oxygen-containing gas, i.e., pressurized oxygen.
In addition, when the injection of the coal water slurry and the second pressurized oxygen-containing gas is started after the gasification of the pulverized coal is stable, the oxygen-coal ratio of the second pressurized oxygen-containing gas to the coal water slurry is within a range from 0.54 Nm3/kg to 0.70 Nm3/kg. In other words, after the gasification of the pulverized coal is stable, the simultaneous injection of the coal water slurry and the second pressurized oxygen-containing gas is started. The ratio of the volume flow (volume unit: Nm3) of the oxygen in the second pressurized oxygen-containing gas to the mass flow (mass unit: kg) of the coal in the coal water slurry injected now is within the range from 0.54 Nm3/kg to 0.70 Nm3/kg.
In the preferred embodiments of the present invention, with regard to the same pressurized oxygen-containing gas, when the “time to start injection” is different, the gas is differentiated by “the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas”. In other words, the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas are the same pressurized oxygen-containing gas. The words “the first and the second” are merely used to define that the two pressurized oxygen-containing gas has different “time to start injection”, instead of defining the pressure or the respective parameter composition thereof. Injection positions of first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas can be preferably different, and same or different injection devices can be used at the same injection position.
In addition, during the injection of the coal water slurry, the mass flow of the coal water slurry is ensured to be greater than or equal to 70% of the load of the first burner 1. Wherein, the load of the first burner 1 is an optimal flow value of a liquid flowing through the burner, and the optimal flow value is already known when a burner leaves the factory.
Here, the pulverized coal and the coal water slurry are co-gasified in the gasifier via the oxygen supply by the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas and the reaction with the pressurized carbon dioxide, to generate a synthesis gas mainly composed of carbon oxide and hydrogen. The synthesis gas is exhausted by the third pipeline 7.
In the foregoing co-gasification process, an operating temperature of the gasifier is controlled within a range from 1400° C. to 1600° C. by adjusting the oxygen-coal ratio of the first pressurized oxygen-containing gas to the pulverized coal to be injected within a range from 0.49 Nm3/kg to 0.65 Nm3/kg and/or by adjusting the oxygen-coal ratio of the second pressurized oxygen-containing gas to the coal water slurry within a range from 0.54 Nm3/kg to 0.70 Nm3/kg.
Specifically, if the operating temperature of the gasifier (i.e., the temperature inside the first chamber 8 of the gasifier) is lower than 1400° C., combustion of the pulverized coal and the coal water slurry inside the gasifier is facilitated by increasing the oxygen-coal ratio of the first pressurized oxygen-containing gas to the pulverized coal to be injected (for example, increasing the volume flow of the oxygen in the first pressurized oxygen-containing gas and/or decreasing the mass flow of the pulverized coal to be injected) and/or by increasing oxygen-coal ratio of the second pressurized oxygen-containing gas to the coal water slurry (for example, increasing the volume flow of the oxygen in the second pressurized oxygen-containing gas and/or decreasing the mass flow of the coal in the coal water slurry). In this way, the operating temperature of the gasifier is increased. If the operating temperature of the gasifier is greater than 1600° C., combustion of the pulverized coal and the coal water slurry inside the gasifier is weakened by decreasing the oxygen-coal ratio of the first pressurized oxygen-containing gas to the pulverized coal to be injected (for example, decreasing the volume flow of the oxygen in the first pressurized oxygen-containing gas and/or increasing the mass flow of the pulverized coal to be injected) and/or by decreasing the oxygen-coal ratio of the second pressurized oxygen-containing gas to the coal water slurry (for example, decreasing the volume flow of the oxygen in the second pressurized oxygen-containing gas and/or increasing the mass flow of the coal in the coal water slurry). In addition, the water phase in the coal water slurry plays a role of decreasing the temperature, and the operating temperature of the gasifier is thus decreased.
In addition, the step 3 of this embodiment also includes a following step: adjusting the operating pressure of the gasifier. In addition, preferably, the operating pressure of the gasifier is controlled within a range from 4.5 MPa to 7.0 MPa.
An operating pressure of the gasifier is controlled by increasing or decreasing a volume flow of oxygen in the first pressurized oxygen-containing gas, a mass flow of the pulverized coal to be injected, a volume flow of oxygen in the second pressurized oxygen-containing gas and a mass flow of coal in the coal water slurry in an equal proportion.
Wherein, it can be understood that there are at least three methods for changing the volume flows of the oxygen in the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas. The first method is that the volume flow of the pressurized oxygen-containing gas is maintained to be constant while the volume flow of oxygen therein is changed so as to change the volume flow of the oxygen. The second method is that the volume flow of the oxygen in the pressurized oxygen-containing gas is maintained unchanged while the volume flow of the pressurized oxygen-containing gas is changed so as to change the volume flow of the oxygen. The third method is a combination of the former two methods. Similarly, there are at least three methods for changing the mass flow of the pulverized coal to be injected. The first method is that the volume flow of the pressurized carbon dioxide gas carrying the pulverized coal to be injected is maintained to be constant while the content of the pulverized coal to be injected therein (mass of the pulverized coal carried in a unit volume of pressurized carbon dioxide gas) is changed so as to change the mass flow of the pulverized coal to be injected which is injected into the gasifier. The second method is that the content of the pulverized coal in the pressurized carbon dioxide gas is maintained unchanged while the volume flow of the pressurized carbon dioxide injected into the gasifier is changed so as to change the mass flow of the pulverized coal. The third method is a combination of the former two methods. Of course, there are at least three methods for changing the mass flow of the coal in the coal water slurry. The first method is that the volume flow of the coal water slurry is maintained to be constant while the content of the coal therein (mass of the coal carried in a unit volume of coal water slurry) is changed so as to change the mass flow of the coal injected into the gasifier. The second method is that the content of coal in the coal water slurry is maintained unchanged while the volume flow of the coal water slurry injected into the gasifier is changed so as to change the mass flow of the coal. The third method is a combination of the former two methods. Any one of the methods may be selected for adjustment, as long as the volume flow of the oxygen in the first pressurized oxygen-containing gas, the mass flow of the pulverized coal to be injected, the volume flow of the oxygen in the second pressurized oxygen-containing gas and the mass flow of the coal in the coal water slurry, which are injected into the gasifier simultaneously, are increased or decreased in an equal proportion. The adjustment methods described above are also applicable to adjustment of the operating temperature and operating pressure during the gasification of the pulverized coal, and to the steps of adjusting the operating temperature of the gasifier in the step 3.
Specifically, in this embodiment, when the operating pressure of the gasifier (the pressure inside the first chamber 8) is lower than 4.5 MPa, the volume flow of the oxygen in the first pressurized oxygen-containing gas, the mass flow of the pulverized coal to be injected, the volume flow of the oxygen in the second pressurized oxygen-containing gas and the mass flow of the coal in the coal water slurry are increased in an equal proportion. For example, both the volume flow of the oxygen in the first pressurized oxygen-containing gas and the mass flow of the pulverized coal, which are injected by the second burner, are increased by 5%, and the volume flow of the oxygen in the second pressurized oxygen-containing gas and the mass flow of the coal in the coal water slurry, which are injected by the first burner, are also increased by 5%, so that an injection amount (the volume flow and the mass flow) of the oxygen and coal (pulverized coal and coal) injected into the gasifier is increased and the amount of synthesis gas generated in the gasifier is increased. In this way, the operating pressure of the gasifier is increased. In addition, in the above adjustment process, the ratio of the volume flow of oxygen in the first pressurized oxygen-containing gas to the mass flow of the pulverized coal to be injected (i.e., oxygen-coal ratio) is constant. Meanwhile, the ratio of the volume flow of oxygen in the second pressurized oxygen-containing gas to the mass flow of the coal in the coal water slurry (i.e., oxygen-coal ratio) is constant. In this way, in the process of adjusting the operating pressure of the gasifier, influence on the operating temperature of the gasifier is weakened.
In contrast, when the operating pressure of the gasifier is greater than 7.0 MPa, the volume flow of the oxygen in the first pressurized oxygen-containing gas, the mass flow of the pulverized coal to be injected, the volume flow of the oxygen in the second pressurized oxygen-containing gas and the mass flow of the coal in the coal water slurry are decreased in an equal proportion. In this way, the amount of the synthesis gas generated is decreased and the operating pressure of the gasifier is further decreased.
It can be understood that, in the embodiments, in a case where the content of oxygen in a unit volume of first pressurized oxygen-containing gas and the content of the oxygen in a unit volume of second pressurized oxygen-containing gas are maintained unchanged, the volume flows of the oxygen in the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas may be increased by increasing the volume flows of the first pressurized oxygen-containing gas and the second pressurized oxygen-containing gas, and vice versa. However, when the mass content of the pulverized coal in a unit volume of pressurized carbon dioxide carrying pulverized coal is maintained unchanged, the mass flow of the pulverized coal may be decreased by decreasing the volume flow of the pressurized carbon dioxide carrying the pulverized coal, and vice versa. In a case where the mass content of the coal in a unit volume of coal water slurry is maintained unchanged, the mass flow of the coal in the coal water slurry may be increased by increasing the volume flow of the coal water slurry, and vice versa. Of course, those skilled in the art can control the pressure and temperature simultaneously. That is, by adjusting the oxygen-coal ratio and adjusting the injection amount in an equal proportion, alternately, the temperature and pressure control is correspondingly realized.
Optionally, the operating pressure of the gasifier may also be increased by reducing the amount of gas passing through the third pipeline 7. In contrast, the operating pressure of the gasifier may be decreased by increasing the amount of gas passing through the third pipeline 7.
Further, in this embodiment, the pulverized coal is injected by carrying it in the pressurized carbon dioxide. On one hand, the participation of carbon dioxide in the co-gasification reaction can increase the content of the effective components of the synthesis gas. On the other hand, the presence of a foreign gas in the synthesis gas is avoided for fear that the following processes might be complicated.
In addition, positions of the first burner 1 and the second burner 2 are not limited to the forgoing embodiments. The first burner 1 and the second burner 2 can be located at any positions of the gasifier as long as the establishment of co-gasification in the gasifier is not influenced. In this embodiment, fuel can be ignited by automatic ignition of the second burner 2 (igniting the combustible gas by supplying a high pressure by an electrode) or by manual ignition (igniting the combustible gas by naked fire). Of course, the way is not limited thereto. Instead, the first pressurized oxygen-containing gas and fuel may be introduced by a nozzle provided on the top of the gasifier, and the fuel in the gasifier may be ignited in other methods well-known to those skilled in the art. In addition, the fuel, the first pressurized oxygen-containing gas and the following pulverized coal can be injected by different devices, not merely limited to by the same burner or nozzle. Also, the coal water slurry and the second pressurized oxygen-containing gas can be injected by a nozzle different from the burner in this embodiment. In addition, the coal water slurry and the second pressurized oxygen-containing gas can be injected by different devices, not merely limited to by the same burner or nozzle. In addition, a plurality of pulverized coal burners and furnace-side burners can be provided, and each of the volume flow and the mass flow mentioned above is a sum of the volume flow or the mass flow of corresponding matters entering by each burner. For example, when two furnace-side burners are provided, the volume flow of oxygen in the second pressurized oxygen-containing gas is a sum of volume flows of oxygen in the second pressurized oxygen-containing gas entering by the two furnace-side burners.
In the second embodiment of the co-gasification of coal of the present invention, a lining of the gasifier is made of firebricks. In the step 3, an operating temperature of the gasifier is controlled within a range from 1300° C. to 1400° C. by adjusting the oxygen-coal ratio of the first pressurized oxygen-containing gas to the pulverized coal to be injected within a range from 0.49 Nm3/kg to 0.65 Nm3/kg and/or by adjusting the oxygen-coal ratio of the second pressurized oxygen-containing gas to the coal water slurry within a range from 0.54 Nm3/kg to 0.70 Nm3/kg. In addition, the operating pressure of the gasifier is controlled within a range from 4.5 MPa to 7.0 MPa (the method is the same as that in the first embodiment). The remaining steps are the same as those in the first embodiment, and will not be repeated here.
In conclusion, the steps disclosed by the present invention facilitate control on the temperature and pressure of the gasifier, with simple operational process, stable operation, quick production and high safety.
The foregoing descriptions are merely preferred embodiments of the present invention, and not intended to limit the present invention. For those skilled in the art, various modifications and changes may be made to the present invention. Any modifications, equivalent replacements, improvements and the like made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.
| Number | Date | Country | Kind |
|---|---|---|---|
| 201410150177.X | Apr 2014 | CN | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/CN2015/076348 | 4/10/2015 | WO | 00 |
