JP4211112B2 - Poor fuel reforming plant and bad fuel reforming method - Google Patents

Description

[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a bad fuel reforming plant and a method for reforming a bad fuel, and more particularly to a technique for improving the quality of a bad fuel with low fluidity or high sulfur content.
[0002]
[Prior art and problems to be solved by the invention]
Inferior fuels such as heavy oil have low fluidity and a high sulfur content. Therefore, when combusting the fuel as it is, a warming fluidizer and an excessive exhaust gas desulfurizer are required. On the other hand, as a fluidization technique or desulfurization technique of fuel, a technique for lightening ultra-heavy oil such as oil sand or oil shale, or a technique for reducing sulfur content in coal is known.
[0003]
However, such conventional technology is an individual technology of ultra-heavy oil lightening technology or sulfur content reduction technology, and is not a technology to fluidize and desulfurize bad fuel as a series of treatment, but to commercialize it. In this case, the processing efficiency is poor and the equipment cost is high.
[0004]
The present invention has been made in view of the above-described problems, and has the following objects.
(1) A poor fuel reforming plant and a method for reforming bad fuel that are low in cost and good in processing efficiency are provided.
(2) A poor fuel reforming plant and a poor fuel reforming method capable of obtaining a reformed fuel with stable quality from bad fuel are provided.
[0005]
[Means for Solving the Problems]
In order to achieve the above object, according to the present invention, as a first means related to a poor fuel reforming plant, the bad fuel flows through a hydrothermal reaction generated in an environment of a temperature of 350 ° C. to 400 ° C. and a pressure of 30 MPa. A pre-stage reactor, a post- stage reactor for desulfurizing the fluidized fuel fluidized by the pre-stage reactor by a hydrothermal reaction generated in an environment of a temperature of 400 ° C. to 450 ° C. and a pressure of 30 MPa , A means comprising fuel component separation means for separating only the fuel component from the desulfurized fuel desulfurized by the reactor and outputting the reformed fuel is employed.
[0006]
Further, as a second means related to the poor fuel reforming plant, in the first means, a torque meter for measuring the pre-reactor inlet torque of the bad fuel at the inlet of the pre-reactor and a flow at the outlet of the pre-reactor. A torque meter for measuring the pre-reactor outlet torque of the liquefied fuel, and the pre-reactor so that the fluidized state of the fluidized fuel maintains the reference state based on the difference between the pre-reactor inlet torque and the pre-reactor outlet torque A means comprising a control device for controlling the progress of the hydrothermal reaction in is adopted.
[0007]
Further, as a third means related to the poor fuel reforming plant, in the first or second means, a sulfur content monitoring sensor for measuring the sulfur content of the reformed fuel, and the desulfurized fuel that has flowed out of the post-reactor. And a recirculation pump for returning the gas to the inlet of the post-reactor, and the control device controls the recirculation pump so that the sulfur content maintains a reference value based on the sulfur content and the pre-reactor outlet torque. The means of configuring is adopted.
[0008]
On the other hand, in the present invention, as a first means related to the reforming method of the poor fuel, the bad fuel is fluidized by a pre-stage hydrothermal reaction that occurs in an environment at a temperature of 350 ° C. to 400 ° C. and a pressure of 30 MPa. The liquefied fluidized fuel is desulfurized by a post- stage hydrothermal reaction that occurs in an environment at a temperature of 400 ° C. to 450 ° C. and a pressure of 30 MPa to obtain a desulfurized fuel, and only the fuel components are separated from the desulfurized fuel and modified. Adopt a means of obtaining quality fuel.
[0009]
Further, as a second means related to the reforming method of the poor fuel, in the first means, the pre-reaction torque of the bad fuel before the pre-stage hydrothermal reaction and the pre-reaction of the fluidized fuel after the pre-stage hydrothermal reaction are used. A means is adopted that measures the torque and adjusts the progress of the pre-stage hydrothermal reaction so that the fluidized state of the fluidized fuel maintains the reference state based on the difference between the pre-stage pre-reaction torque and the pre-stage post-reaction torque.
[0010]
Further, as a third means related to the reforming method of the poor fuel, in the first or second means, the sulfur content of the reformed fuel is measured and one of the desulfurized fuel after the post-stage hydrothermal reaction is measured. The post-stage hydrothermal reaction is performed again, and the amount of desulfurized fuel to be subjected to the post-stage hydrothermal reaction again is adjusted based on the sulfur content and the post-stage post-reaction torque so that the sulfur content maintains the reference value. Adopt means.
[0011]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, an embodiment of a poor fuel reforming plant and a poor fuel reforming method according to the present invention will be described with reference to the drawings. This embodiment relates to reforming heavy oil (bad fuel) used for fuel in a thermal power plant.
[0012]
FIG. 1 is a system configuration diagram of a poor fuel reforming plant in the present embodiment. As shown in this figure, this poor fuel reforming plant includes a fuel tank 1 for storing heavy oil X, a preheater 2, a fuel discharge pump 3, addition devices 4 and 5, a mixing heater 6, a pressure pump 7, Heater 8, torque meter 9, 10, pre-reactor 11, post-reactor 12, recirculation pump 13, orifices 14, 15, oil separator 16 (fuel component separator), sulfur monitor sensor 17 and controller 18 Etc.
[0013]
The poor fuel reforming plant configured as described above is provided as an accessory facility of the thermal power plant, and as described below, by effectively utilizing the exhaust gas of the boiler of the thermal power plant, the heavy oil reforming plant is improved. It is configured to reduce energy consumption related to quality as much as possible.
[0014]
The fuel tank 1 stores heavy oil X in an amount commensurate with the fuel consumption of the thermal power plant. The heavy oil X contains, for example, about 5% sulfur. Only the heavy oil X with a sulfur content within a certain range, that is, around 5%, is supplied to the thermal power plant from the outside.
[0015]
The preheater 2 is provided on the outer periphery of the fuel tank 1 and preheats the heavy oil X to about 70 ° C. The fuel discharge pump 3 discharges the heavy oil X in the preheated state as described above from the fuel tank 1, and its operation is controlled by the control device 18.
[0016]
The adding device 4 adds an additive to the heavy oil X discharged from the fuel discharge pump 3. This additive is an organic solvent such as ethanol, acetone, toluene or hexane and ammonia (NH ₃ ), and is for accelerating the subsequent reaction in the pre-stage reactor 11 and the post-stage reactor 12.
[0017]
The adding device 5 adds a gas additive to the heavy oil X discharged from the fuel discharge pump 3. This gas additive is, for example, carbon monoxide (CO), and is for accelerating the reaction in the pre-stage reactor 11 and the post-stage reactor 12.
[0018]
The mixing heater 6 is provided to heat the organic solvent and carbon monoxide so as to be uniformly mixed in the heavy oil X and to add moisture to the heavy oil X. The mixing heater 6 adds the auxiliary steam from the boiler of the thermal power plant to the heavy oil X to which the organic solvent and carbon monoxide are added, thereby heating the heavy oil X and adding water. Do.
[0019]
The pressurizing pump 7 is for pressurizing the heavy oil X (added with water, organic solvent and carbon monoxide) output from the mixing heater 6 to a pressure of about 30 MPa, and its operation is controlled. It is controlled by the device 18.
[0020]
The heater 8 uses the auxiliary steam from the boiler of the thermal power plant and the steam discharged from the oil separator 16 as a heat source, so that the heavy oil X discharged from the pressurizing pump 7 is about 330 ° C. It is for heating.
[0021]
The torque meter 9 measures the flow torque of the heavy oil X at the heater outlet of the heated heavy oil X (that is, the inlet of the front reactor 11), and the measured value (the front reactor inlet torque, (Pre-reaction torque) is output to the control device 18. The torque meter 10 measures the flow torque of the heavy oil X at the outlet of the pre-reactor 11 (that is, the inlet of the post-reactor 12), and the measured values (pre-reactor outlet torque, pre-reaction post-reaction torque). This is output to the control device 18.
[0022]
The pre-stage reactor 11 is provided with a pipe having a predetermined length through which the heavy oil X introduced from the heater 8 is passed, and the heavy oil X in the pipe is exhausted from the exhaust gas of the boiler of the thermal power plant. It is configured to heat to about 350 ° C. to 400 ° C.
[0023]
That is, in the pre-stage reactor 11, the heavy oil X (water, organic solvent, ammonia and carbon monoxide added) flowing in from the inlet is at a temperature of 350 ° C. to 400 ° C. and a pressure in the pipe. As the lightening oil Xa (fluidized fuel), the polymer component of the heavy oil X is reduced in molecular weight by the hydrothermal reaction (previous hydrothermal reaction) that occurs in an environment of 30 MPa. Output from the outlet of the pre-reactor 11.
[0024]
The post-stage reactor 12 is provided with a pipe having a predetermined length through which the lightened oil Xa introduced from the heater 8 is sent, as in the case of the pre-stage reactor 11, and the lightened oil Xa in the pipe is provided. Is heated to about 400 ° C. to 450 ° C. by the exhaust gas from the boiler of the thermal power plant.
[0025]
In this post-stage reactor 12, the lightened oil Xa flowing from the pre-stage reactor 11 is subjected to a hydrothermal reaction (post-stage hydrothermal reaction) in the pipeline that occurs in an environment of a temperature of 400 ° C. to 450 ° C. and a pressure of 30 MPa. The molecular bond between carbon (C) and sulfur (S) is cut, and desulfurized desulfurized oil Xb (desulfurized fuel) is output from the outlet of the rear reactor 12. At this time, sulfur (S) separated from the lightened oil Xa reacts with hydrogen (H ₂ ) generated by the reaction of water (H ₂ O) and carbon monoxide (CO), thereby producing hydrogen sulfide (H ₂ S).
[0026]
The recirculation pump 13 returns the desulfurized oil Xb thus output from the rear reactor 12 to the inlet of the rear reactor 12. The orifice 14 is for depressurizing the desulfurized oil Xb output from the post-stage reactor 12 to 10 MPa and supplying it to the oil separator 16. On the other hand, the orifice 15 discharges the auxiliary steam from the boiler of the thermal power plant supplied as a heat source to the heater 8 and the steam discharged from the oil separator 16 to the atmospheric pressure.
[0027]
The oil separator 16 separates only the oil (fuel component) from the desulfurized oil Xb decompressed to about 10 MPa by the orifice 14 and sends it to the thermal power plant with a pressure of about 6 MPa. The desulfurized oil Xb contains water, hydrogen sulfide (H ₂ S) produced in the latter reactor 12, and ammonium sulfide [(NH ₃ ) produced by the reaction of ammonia (NH ₃ ) and sulfur (S). ₂ S] and the like are contained, but by reducing the pressure to about 10 MPa at the orifice 14, water, sulfur content such as hydrogen sulfide (H ₂ S) and ammonium sulfide [(NH ₃ ) ₂ S], and water become gas. Only the oil is in a liquid state.
[0028]
The oil separator 16 separates only the liquid oil from the desulfurized oil Xb and sends it to the thermal power plant as reformed oil Xc (reformed fuel), and water containing other sulfur (water vapor) ) Is supplied to the heater 8. Here, the sulfur (S) separated from the desulfurized oil Xb finally reacts with hydrogen (H ₂ ) generated by the reaction of water (H ₂ O) and carbon monoxide (CO), thereby finally. It is supplied to the heater 8 as ammonium sulfate.
[0029]
The sulfur content monitoring sensor 17 is for detecting the sulfur content contained in the reformed oil Xc thus generated, and outputs this detected value (sulfur content) to the control device 18. The control device 18 monitors and controls the operation of the present poor fuel reforming plant.
[0030]
For example, the control device 18 is configured to input the upstream reactor inlet torque input from the torque meter 9, the upstream reactor outlet torque input from the torque meter 10, and the sulfur of the reformed oil Xc input from the sulfur content monitoring sensor 17. Based on the content, the operations of the fuel discharge pump 3, the pressurizing pump 7, and the recirculation pump 13 are controlled. The control operation of the control device 18 will be described in detail below.
[0031]
Next, the operation of the present poor fuel reforming plant will be described in detail.
During the steady operation of this poor fuel reforming plant, the control device 18 controls the fuel discharge pump 3 so as to discharge the heavy oil X having a flow rate corresponding to the consumption of the thermal power plant from the fuel tank 1, and The pressurizing pump 7 and the recirculation pump 13 are controlled as follows. The addition amounts of the organic solvent and carbon monoxide in the addition apparatuses 4 and 5 and the addition amount of water vapor in the mixing heater 6 are set to predetermined values according to the amount of heavy oil X discharged.
[0032]
First, for the pressurizing pump 7, the control device 18 discharges the heavy oil X (compression amount) based on the difference between the upstream reactor inlet torque of the torque meter 9 and the upstream reactor outlet torque of the torque meter 10. And the temperature of the pre-reactor 11 is controlled. That is, the difference between the pre-reactor inlet torque and the pre-reactor outlet torque is an amount indicating the degree of fluidization of the heavy oil X in the pre-reactor 11, that is, the progress of the hydrothermal reaction in the pre-reactor 11. is there.
[0033]
When the hydrothermal reaction in the pre-reactor 11 is sufficiently advanced, the pre-reactor outlet torque at the outlet of the pre-reactor 11 is decreased, and the hydrothermal reaction in the pre-reactor 11 is not sufficiently proceeding. In this case, the upstream reactor outlet torque increases. Therefore, the difference between the upstream reactor inlet torque and the upstream reactor outlet torque is an amount indicating the degree of fluidization of the heavy oil X in the upstream reactor 11.
[0034]
When the difference between the upstream reactor inlet torque and the upstream reactor outlet torque is smaller than the reference value, that is, when the heavy oil X is not sufficiently fluidized in the upstream reactor 11, the control device 18. The pressurizing pump 7 is controlled so as to increase the discharge amount (compression amount) of the heavy oil X to increase the pressure. As a result, the hydrothermal reaction in the pre-stage reactor 11 proceeds more than ever, and the fluidized state of the heavy oil X at the outlet of the pre-stage reactor 11 is maintained in the reference state. The progress of the hydrothermal reaction can also be promoted by increasing the temperature of the pre-reactor 11.
[0035]
On the other hand, the control device 18 controls the recirculation pump 13 based on the upstream reactor outlet torque of the torque meter 10 and the sulfur content of the sulfur content monitoring sensor 17. That is, when the sulfur content exceeds the reference value, that is, when the hydrothermal reaction in the post-reactor 12 does not proceed sufficiently and the pre-reactor outlet torque is maintained at the reference value, the pre-reactor Although the hydrothermal reaction in 11 is sufficient, the hydrothermal reaction in the post-stage reactor 12 is insufficient.
[0036]
In such a case, the control device 18 controls the recirculation pump 13 so that the desulfurized oil Xb at the outlet of the rear reactor 12 is returned to the inlet more than the reference amount. As a result, more desulfurized oil Xb flows again into the post-reactor 12, so that the separation of the sulfur component is promoted, and the sulfur content of the sulfur content monitoring sensor 17 is maintained at the reference value.
[0037]
The flow rate of the heavy oil X discharged from the fuel tank 1 according to the consumption of the thermal power plant, that is, the flow rate of the heavy oil X flowing into the front reactor 11 and the light oil Xa flowing into the rear reactor 12 varies. However, by controlling the pressurization pump 7 and the recirculation pump 13 by the control device 18 as described above, the fluidization state and sulfur content of the reformed oil Xc sent to the thermal power plant are determined according to a predetermined standard. Maintained at the value.
[0038]
According to this embodiment, the heavy oil X is fluidized by the hydrothermal reaction in the pre-stage reactor 11, and the fluidized lightened oil Xa is hydrothermally reacted in the post-stage reactor 12 to separate the sulfur content. To do. That is, the state in which the contact area between water and heavy oil X is improved by reducing the molecular weight (fluidization) of heavy oil X in the pre-stage reactor 11 to improve the mixing property of water and heavy oil X. Thus, since the sulfur content is separated by the hydrothermal reaction of the post-stage reactor 12, the sulfur content can be easily separated in the post-stage reactor 12. Therefore, compared with the case where heavy oil X is directly desulfurized, the reaction time in the subsequent reactor 12, that is, the reaction time related to desulfurization can be shortened, so that the heavy oil X can be reformed (fluidized) in a shorter time. And desulfurization).
[0039]
In addition, since the heavy oil X is reformed by the continuous treatment of the pre-stage reactor 11 and the post-stage reactor 12, the equipment cost can be reduced. Furthermore, since the auxiliary steam and exhaust gas of the thermal power plant are used, energy consumption can be reduced.
[0040]
【The invention's effect】
As described above, the bad fuel reforming plant and the bad fuel reforming method according to the present invention have the following effects.
(1) A pre-reactor that fluidizes bad fuel by hydrothermal reaction, a post-reactor that desulfurizes fluidized fuel fluidized by the pre-reactor by hydrothermal reaction, and desulfurized by the post-reactor Since the fuel component separating means for separating only the fuel component from the desulfurized fuel and outputting the reformed fuel is provided, reforming of the poor fuel fluidization and desulfurization can be realized as a series of processing equipment. Therefore, the cost can be reduced and the processing efficiency can be improved.
(2) A torque meter for measuring the pre-reactor inlet torque of the bad fuel at the inlet of the pre-reactor, a torque meter for measuring the pre-reactor outlet torque of the fluidized fuel at the outlet of the pre-reactor, and the pre-reactor inlet Since the control device controls the progress of the hydrothermal reaction in the front reactor so that the fluidized state of the fluidized fuel maintains the reference state based on the difference between the torque and the front reactor outlet torque, the fluidization quality Uniform reformed fuel can be obtained.
(3) A sulfur content monitoring sensor for measuring the sulfur content of the reformed fuel, and a recirculation pump for returning the desulfurized fuel flowing out from the rear reactor to the inlet of the rear reactor, the sulfur content and the front reactor By configuring the control device to control the recirculation pump so that the sulfur content maintains the reference value based on the outlet torque, a reformed fuel with uniform desulfurization quality can be obtained.
[Brief description of the drawings]
FIG. 1 is a system configuration diagram of a poor fuel reforming plant according to an embodiment of the present invention.
[Explanation of symbols]
DESCRIPTION OF SYMBOLS 1 ... Fuel tank 2 ... Preheater 3 ... Fuel delivery pumps 4, 5 ... Addition device 6 ... Mixing heater 7 ... Pressurizing pump 8 ... Heaters 9, 10 ... Torque meter 11 ... Preceding Reactor 12... Reactor 13... Recirculation pumps 14 and 15. Orifice 16... Oil separator (fuel component separation means)
17 ... Sulfur content monitoring sensor 18 ... Control device X ... Heavy oil (poor fuel)
Xa: Lighter oil (fluidized fuel)
Xb: Desulfurized oil (desulfurized fuel)
Xc: reformed oil (reformed fuel)

Claims (6)

A pre-stage reactor (11) for fluidizing the crude fuel (X) by a hydrothermal reaction occurring in an environment at a temperature of 350 ° C. to 400 ° C. and a pressure of 30 MPa ;
A post- reactor (12) for desulfurizing the fluidized fuel (Xa) fluidized by the pre- reactor (11) by a hydrothermal reaction that occurs in an environment at a temperature of 400 ° C. to 450 ° C. and a pressure of 30 MPa ;
Fuel component separation means (16) for separating only the fuel component from the desulfurized fuel (Xb) desulfurized by the latter reactor (12) and outputting the reformed fuel (Xc);
A poor fuel reforming plant characterized by comprising:   Torque meter (9) for measuring the pre-reactor inlet torque of the poor fuel (X) at the inlet of the pre-reactor (11), and the pre-reactor outlet of the fluidized fuel (Xa) at the outlet of the pre-reactor (11) A torque meter (10) for measuring torque, and a pre-reactor (Xa) so that the fluidized state of the fluidized fuel (Xa) maintains the reference state based on the difference between the pre-reactor inlet torque and the pre-reactor outlet torque. The poor fuel reforming plant according to claim 1, further comprising a control device (18) for controlling the progress of the hydrothermal reaction in (11).   A sulfur content monitoring sensor (17) for measuring the sulfur content of the reformed fuel (Xc) and a recirculation for returning the desulfurized fuel (Xb) flowing out from the rear reactor (12) to the inlet of the rear reactor (12) A pump (13), and the controller (18) controls the recirculation pump (13) so that the sulfur content maintains a reference value based on the sulfur content and the pre-reactor outlet torque. The inferior fuel reforming plant according to claim 1 or 2. The crude fuel (X) is fluidized by a pre-stage hydrothermal reaction that occurs in an environment of a temperature of 350 ° C. to 400 ° C. and a pressure of 30 MPa, and the fluidized fluidized fuel (Xa) is heated to a temperature of 400 ° C. to 450 ° C. C. Desulfurization is performed by a post- stage hydrothermal reaction that occurs in an environment with a pressure of 30 MPa to obtain a desulfurized fuel (Xb), and only a fuel component is separated from the desulfurized fuel (Xb) to obtain a reformed fuel (Xc). A method for reforming poor fuel, characterized by   The pre-reaction torque of the poor fuel (X) before the pre-stage hydrothermal reaction and the pre-reaction torque of the fluidized fuel (Xa) after the pre-stage hydrothermal reaction are measured, and the difference between the pre-reaction torque and the pre-reaction torque 5. The method for reforming an inferior fuel according to claim 4, wherein the progress of the pre-stage hydrothermal reaction is adjusted so that the fluidized state of the fluidized fuel (Xa) maintains the reference state based on the above.   The sulfur content of the reformed fuel (Xc) is measured, and a part of the desulfurized fuel (Xb) after the post-stage hydrothermal reaction is caused to react again with the post-stage hydrothermal reaction. 6. The method for reforming a poor fuel according to claim 4, wherein the amount of the desulfurized fuel (Xb) to be subjected to the subsequent hydrothermal reaction is adjusted again so that the sulfur content maintains the reference value based on the above.

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