JP6681316B2 - Method and apparatus for removing acid component at high temperature in gasification power generation system - Google Patents

Description

  INDUSTRIAL APPLICABILITY The present invention uses a combustible gas obtained by gasifying and reforming waste to generate electricity in a gas turbine or a gas engine, and removes acid components in a high-temperature gasified gas with a high removal rate. It relates to a method of achieving and an apparatus used to carry out the method.

  In recent years, there has been a strong demand for countermeasures against global warming, and even in power generation using waste, power generation efficiency has been improved by raising the steam temperature of waste incineration power generation (BTG power generation), and waste has been gasified and reformed. A system for generating power by a gas turbine or a gas engine using combustible gas has been studied.

  In such a power generation system, gasification of incombustibles and various metals, particularly waste containing metal aluminum, is generally performed at 700 ° C or lower, usually at about 500 to 650 ° C. In the gasification gas, unburned char and tar components are reformed into combustible gas by steam in the reforming furnace. The reforming reaction is carried out at about 1000 to 1200 ° C. when it is carried out without a catalyst, and at about 800 to 1000 ° C. when a catalyst is used.

  For example, Patent Document 1 describes a gasification power generation system including a gasification furnace, high-temperature dust collection equipment, tar decomposition equipment, refining equipment, and the like. In this gasification power generation system, after the gas at 800 to 900 ° C. generated in the gasification furnace is dedusted by the high temperature dust collector equipped with a ceramic filter or the like, the tar decomposition facility equipped with a decomposition catalyst for tar etc. Sent.

In the gas obtained by gasifying waste, in addition to unburned char and tar, flammable gases such as H ₂ , CH ₄ , and CO, CO ₂ and dust, HCl derived from halogen and S contained in waste, and HCl And SO ₂ and SO ₃ gas are included.

When a reforming reaction is carried out using a catalyst, a nickel-based or noble metal-based reforming catalyst is used, but the reforming catalyst is covered by HCl, SO ₂ or SO ₃ gas contained in the gasified gas. Be poisoned. In order to prevent such poisoning of the reforming catalyst, it is necessary to remove poisonous gas components upstream of the reforming furnace. However, in the high temperature dust collector described in Patent Document 1, only the dust is removed and desalting and desulfurization are not performed, so that the performance of the decomposition catalyst such as tar content may be deteriorated.

Conventionally, as a desalination / desulfurization technology for a waste incineration system using a dry method, a powdery chemical such as slaked lime (Ca (OH) ₂ ) or baking soda (NaHCO ₃ ) is blown into the exhaust gas flow to generate a solid reaction. A technique of removing an object with a bag filter is known. This technique is applied to the exhaust gas temperature range of 150 to 200 ° C., and the lower the temperature, the better the removal efficiency. In addition, a technique for purifying a pyrolysis gas by applying such a technique is disclosed (Patent Document 2). One of the techniques disclosed in Patent Document 2 is that the pyrolysis gas is purified by a dust removing bag filter and a desalting second bag filter. Dust-removed pyrolysis gas is mixed with alkaline agents such as slaked lime, calcium oxide (CaO), calcium carbonate, baking soda, and sodium carbonate (Na ₂ CO ₃ ) before the second bag filter, and HCl is added to the second bag filter. It is removed as a solid reaction product at 300 to 600 ° C., which is close to the thermal decomposition temperature range. However, HCl competes with carbon dioxide in this temperature range, and many chemicals are required to obtain a high HCl removal rate. Further, since the bag filter for removing dust does not perform desalting and desulfurization, there is a possibility that purification of the pyrolysis gas may be insufficient.

Further, there is disclosed a sodium aluminate (NaA1O ₂ ) -based halide absorbent produced by pulverizing and firing a mixture of sodium carbonate and alumina sol after drying (Patent Document 3). The particle size of this halide absorbent is 250 to 500 μm, and in Patent Document 3, the halide removal performance is evaluated at 400 ° C. using a fixed bed flow reactor. However, if a fixed bed flow reactor is installed in the pyrolysis gas flue of waste in a temperature range of less than 500 ° C and dry desalination / desulfurization is performed, tar is attached to dust and char and is fixed. It adheres to the halogenated absorbent in the bed flow reactor, and pressure loss increases due to clogging, making stable operation impossible. For example, in a filtration test using polystyrene as an oil component (tar component), the polystyrene adheres to the filter, and when the polystyrene attached to the filter is heat-treated at a temperature of 500 ° C. or higher, the oil is removed and the pressure loss is reduced. It has been reported to return (Non-Patent Document 1).

JP, 2006-037012, A JP, 2002-130628, A Japanese Patent No. 3571219

Shoichi Ogawa, et al., Collection and regeneration characteristics of hydrocarbon components of polystyrene pyrolysis gas by ceramic filter, Journal of Powder Engineering, Vo 1.40 No. 11, p19-25, 2003

  The present invention can achieve high desalination / desulfurization performance in a high temperature range in order to solve the above-mentioned problems of the prior art, and the pressure loss due to clogging of the device due to tar deposits on dust or char. It is an object of the present invention to provide a method and an apparatus for removing an acid component at high temperature in a gasification power generation system, which does not cause a rise in temperature.

  The present invention has been made to achieve the above object and includes the following aspects.

(1) A gasification step of partially combusting a gasification material, a cyclone treatment step of collecting coarse gas from the gasification gas discharged from the gasification step, and a removal of coarse powder from the cyclone treatment step a bag filter processing step of dust removal processing gasification gas, the bag filter exits the process dust already gasification gas and CO ₂ absorption reforming step of treating the CO ₂ absorbing reforming, the CO ₂ absorption and modification In a gasification power generation system including a power generation process for generating power using reformed gas from the process,
After the gasification step and before the cyclone treatment step, a cyclone upstream additive having a desalination / desulfurization function is used as an additive carrier gas after the heat recovery of the gas generated from the power generation step to produce a gasification gas. Supply to, and
When the CO ₂ absorber used in the CO ₂ absorbing and reforming process gas temperature range 450-700 ° C., preferably of is CO ₂ absorption in a temperature range of five hundred and forty to six hundred and forty ° C., CO ₂ absorption amount reaches saturation, Kai The flow of oxygen or air for raising the quality catalyst layer is switched to immediately upstream of the CO ₂ absorbent packed bed, and the absorbent packed bed is heated to a temperature range of 800 to 950 ° C, preferably 850 to 900 ° C. CO ₂ is released from the absorbent,
A method for removing an acid component at high temperature in a gasification power generation method.

(2) The acid component removal method at high temperature in the gasification power generation method according to (1), wherein the cyclone upstream additive also has a CO ₂ absorption / removal function.

  (3) The method for removing an acid component at high temperature in the gasification power generation method according to (1) or (2), wherein the cyclone upstream additive has an average particle size of 100 to 1000 μm.

  (4) The gasification according to any one of (1) to (3), wherein the cyclone upstream additive is selected from the group consisting of calcined dolomite, slaked lime, sodium aluminate and baking soda. A method for removing an acid component at high temperature in a power generation method.

  (5) After the cyclone treatment step and before the bag filter treatment step, a cyclone downstream additive having a desalination / desulfurization function and may be the same as or different from the cyclone upstream additive. However, an additive selected from the group consisting of calcined dolomite, slaked lime, sodium aluminate and baking soda is used as an additive carrier gas after heat recovery of the gas from the power generation step, and the coarse powder removed gasification gas. The method for removing an acid component at high temperature in the gasification power generation method according to any one of (1) to (4), characterized in that

  (6) In the cyclone treatment step, the coarse powder containing the additive is collected, and the collected coarse powder is supplied to the gasification step together with the gasification material, (1) ~ A method for removing an acid component at high temperature in the gasification power generation method according to any one of (5).

(7) the CO ₂ absorbing agent used in the CO ₂ absorption and the reforming step, characterized in that the member selected from the group consisting of CaO, Ca _{(OH) 2} and burnt dolomite, either (1) to (6) A method for removing an acid component at high temperature in the gasification power generation method according to 1.

(8) In any one of (1) to (7), the reformed gas is subjected to CO ₂ absorption treatment with an aqueous NaOH solution after heat recovery treatment to collect and remove generated Na ₂ CO _3. A method for removing an acid component at high temperature in the gasification power generation method as described.

(9) A gasification furnace that partially gasifies the gasification material, a cyclone that is installed downstream of the gasification furnace and that collects the gasification gas from the furnace that collects coarse powder, and a cyclone that is downstream of the cyclone. a bag filter installed to dust removal processing exiting crude powder-removed gasification gas from here, the installed downstream of the bag filter dust removal has been gasified gas from here to process the CO ₂ absorbing reforming CO ₂ In a gasification power generation system including an absorption / reformation furnace and a power generation facility installed downstream of the CO ₂ absorption / reformation furnace to generate electric power using a reformed gas discharged from the furnace,
A cyclone upstream additive supply line for supplying an additive having a desalination / desulfurization function is provided in the flow path from the gasification furnace to the cyclone, and the carrier gas line coming from the power generation facility is connected to the supply line. It is, switching the oxygen or air for the reforming RoNoboru temperature to CO ₂ absorbent filler layer when CO ₂ absorption immediately upstream of the CO ₂ absorption and reformer CO ₂ absorbent filler layer reaches saturation Characterized in that an oxygen or air supply line is connected,
High temperature acid component removal device in gasification power generation system.

(10) A cyclone downstream additive supply line for supplying an additive having a desalination / desulfurization function is provided in the flow path from the cyclone to the bag filter, and the carrier gas line coming from the power generation facility is provided in the supply line. Is connected,
An acid component removing device at high temperature in the gasification power generation system according to (9).

  The average particle size of the particles is a value measured by a laser diffraction type particle size distribution measuring device.

  Throughout the specification and claims, the gas obtained by partial combustion gasification of a gasification material is referred to as [gasification gas].

  According to the present invention, by supplying the cyclone upstream additive having a desalination / desulfurization function to the gasification gas before the cyclone treatment step, and further before the bag filter treatment step, the desalination / desulfurization function is provided. By supplying the cyclone downstream-side additive having a gasification gas to the gasification gas, high desalination / desulfurization performance can be achieved for the gasification gas in a high temperature range of 450 to 700 ° C. Poison can be prevented.

  Further, by using the additive as described above, it is possible to prevent the problem that the tar content is attached to dust or char and the pressure loss increases due to clogging of the device.

Furthermore, the CO ₂ absorbing agent used in the CO ₂ absorption and reforming process is CO ₂ absorption at gas temperature range 450-700 ° C., when the CO ₂ absorption amount reaches saturation, oxygen or for the reforming catalyst SoNoboru temperature In the gasification gas, by switching the flow of air to immediately upstream of the CO ₂ absorbent packed bed and raising the temperature of the absorbent packed bed to a temperature range of 800 to 900 ° C. to separate CO ₂ from the absorbent. CO ₂ can be efficiently and permanently removed.

FIG. 1 is a flow chart of a gasification power generation system showing an embodiment of the present invention. FIG. 2 is a graph and a table showing the relationship between the desalination / desulfurization agent and the desalination / desulfurization performance. FIG. 3-1 is a graph showing the relationship between various desalination / desulfurization agents and desalination / desulfurization performance (temperature: 550 ° C.). FIG. 3-2 is a graph showing the relationship between various desalination / desulfurization agents and desalination / desulfurization performance (temperature: 600 ° C.). FIG. 3-3 is a graph showing the relationship between various desalination / desulfurization agents and desalination / desulfurization performance (temperature: 650 ° C.).

  An embodiment of the present invention will be described with reference to the accompanying drawings. However, this does not limit the present invention.

  First, the gasification power generation system will be described with reference to FIG.

The gasification power generation system includes a gasification furnace 1 for partial combustion gasification of a gasification material, a bag filter 3 installed downstream of the gasification furnace 1 for removing gasification gas from the furnace, and a bag filter 3. Power is generated using a CO ₂ absorption / reformation furnace 4 that is installed downstream to reform the dust-removed gas and a reformed gas that is installed downstream from the CO ₂ absorption / reformation furnace 4 And a power generation facility 5 for performing.

A cyclone 2 is installed in a flow path from the gasification furnace 1 to the bag filter 3, and an additive having a desalination / desulfurization function and preferably a CO ₂ removal function is provided in an upstream side flow path of the cyclone 2. A cyclone upstream side additive supply line 6 for supplying the additive from the additive container 8 is connected. Further, a cyclone downstream side additive supply line 7 for supplying an additive having a desalination / desulfurization function and preferably a CO ₂ removal function from the additive container 10 in the flow path from the cyclone 2 to the bag filter 3. Is provided.

  At the starting ends of the cyclone upstream side additive supply line 6 and the cyclone downstream side additive supply line 7, a carrier gas line 9 is provided from the power generation facility 5 via the low temperature boiler 13, the dehumidifier 14, the booster 15 and the tank 16. It is connected.

Immediately upstream of the CO ₂ absorbent filler layer of the CO ₂ absorption and reformer 4, CO ₂ absorbent filler layer flow of oxygen or air for reforming RoNoboru temperature when the CO ₂ absorbing amount reaches the saturated An oxygen or air supply line 19 for switching to is connected. The line 19 normally supplies oxygen or air for temperature raising just upstream of the catalyst packed bed of the CO ₂ absorption / reforming furnace 4.

Next, the method for removing an acid component at high temperature in the gasification power generation method according to the present invention will be specifically described for each step according to the flowchart of FIG.
Gasification process Gasification materials such as waste, RDF, and wood chips are partially combusted and gasified in the gasification furnace 1. Oxygen and water vapor are supplied to the gasification furnace 1 from the bottom of the furnace.

Cyclone treatment step The gasification gas discharged from the top of the gas furnace 1 is sent to the cyclone 2, and the particles in the gasification gas are divided into coarse powder having an average particle size of 100 μm or more and fine powder having an average particle size of less than 100 μm. . The temperature of the gas entering the cyclone 2 is 700 ° C or lower, preferably 550 to 650 ° C, and the temperature of the gas exiting the cyclone 2 is 550 to 650 ° C.

An additive having a desalination / desulfurization function is blown into the upstream channel of the cyclone 2 through the cyclone upstream additive supply line 6. This additive preferably also has a CO ₂ absorption / removal function in addition to a desalination / desulfurization function. It can be converted to chloride or sulfate at 700 ° C. or lower, and is preferably selected from the group consisting of calcined dolomite, slaked lime, sodium aluminate and baking soda. The average particle size of the additive is preferably 100 to 1000 μm, more preferably 300 to 600 μm. Calcined dolomite is preferable in terms of cost, and sodium aluminate is preferable in terms of desalination / desulfurization rate. In this example, calcined dolomite having an average particle size of several hundred μm was fed from additive container 8 via line 6 upstream of the cyclone.

By blowing an additive having a desalination / desulfurization function, preferably a CO ₂ absorption / removal function, into the upstream channel of the cyclone 2, the gasification gas is desalted / desulfurized, preferably decarbonated. In addition to being able to process, the dust and tar adhering in the cyclone 2 can be self-cleaned, the pressure loss in the downstream bag filter can be suppressed, and the operation can be performed without any trouble. Part or all of the coarse powder additive having an average particle size of 100 to 1000 μm, dust, and tar are recovered at the bottom by the cyclone, and the recovered product is supplied to the gasification furnace 1 together with the gasification material. Thereby, the reforming of tar in the CO absorption / reforming furnace 4 located downstream can be complemented.

Bag filter treatment step The coarse powder-removed gasified gas from the cyclone 6 is then sent to the bag filter 3 that removes dust from the gas. The gasification gas from which the coarse powder has been removed contains particles having an average particle size of less than 100 μm.

An additive having a desalination / desulfurization function is blown into the flow path from the cyclone 2 to the bag filter 3 by the cyclone downstream side additive supply line 7. This additive preferably has a CO ₂ absorption / removal function in addition to the desalination / desulfurization function. This additive can be converted into chloride or sulfate at 700 ° C. or lower, and is preferably selected from the group consisting of calcined dolomite, slaked lime, sodium aluminate and baking soda. The average particle size of the additive is preferably 20 μm or less, more preferably 15 μm or less. Calcined dolomite is preferable in terms of cost, and sodium aluminate is preferable in terms of desalination / desulfurization rate. The cyclone downstream additive may be the same as or different from the cyclone upstream additive. In this example, calcined dolomite having an average particle size of 20 μm or less was supplied from the additive tank 10 to the cyclone downstream side by the cyclone downstream side additive supply line 7.

By blowing an additive having a desalination / desulfurization function, preferably a CO ₂ absorption / removal function, into the downstream channel of the cyclone 2, the gasification gas from which the coarse powder has been removed is desalted / desulfurized. Preferably, decarboxylation treatment can be performed. In particular, the desalination / desulfurization treatment can extend the life of the Ni-based reforming catalyst generally used in the downstream CO ₂ absorption / reforming furnace 4.

  The average particle size of the additive is preferably 20 μm or less in order to enhance the effects of desalination and desulfurization. A known filter aid may be used in combination with the cyclone downstream additive.

  The average particle size of the particles is a value measured by a laser diffraction type particle size distribution measuring device.

In this embodiment, as the bag filter 3, a pre-coated bag filter is used to prevent dust containing tar content from adhering to the filter cloth and to improve the peelability of the cake layer on the surface of the filter cloth. The temperature of the gas entering the precoat bag filter is 550 to 650 ° C, and the temperature of the gas exiting the bag filter falls to about 540 to 640 ° C due to heat radiation or the like. When the pressure loss in the pre-coated bag filter becomes large, the cake layer on the surface of the filter cloth is wiped off by the pulse jet method, and then the cyclone downstream side additive or a combination of the additive and the filter aid is used for a short time. Then, pre-coat on the surface of the filter cloth. The pressure loss during precoating is set to 0.5 to 0.6 kPa. The cake layer on the surface of the filter cloth is wiped off when the pressure loss is preferably in the range of 1.5 to 1.8 kPa (153.0 to 183.5 mmH ₂ O).

As for the amount of precoat, 3 equivalents of HCl + SO ₂ in gas are blown in for about 20 minutes. As a guideline, the total of the time required for precoating and the steady operation time is about 3.5 hours as one cycle. Discharge by pulse jet is preferably done by pressure loss control of the bag.

CO ₂ Absorption / Reforming Step The gasified gas is sent to the CO ₂ absorption / reforming furnace 4 after being dedusted by the bag filter 3. The upper part of the CO ₂ absorption / reforming furnace 4 is filled with a CO ₂ absorbent, and the lower part is filled with a reforming catalyst. As a CO ₂ absorbent, carbonation by CO ₂ absorption proceeds in the temperature range of 450 to 700 ° C., preferably 540 to 640 ° C., and decarboxylation, ie, CO in the temperature range of 800 to 950 ° C., preferably 850 to 900 ° C. _{2 A} compound that causes elimination is used. Examples of the CO ₂ absorbent include CaO, Ca (OH) ₂ and calcined dolomite (CaO.MgO). In this example, CaO was used as the CO ₂ absorbent.

The described CO ₂ desorption from CO ₂ absorbent by switching the oxygen or the flow path of the air supply line 19.
1) During normal CO ₂ absorption operation, the temperature range of the gasification gas is 450 to 700 ° C., preferably 540 to 640 ° C., and the temperature of the CO ₂ absorbent is also kept in this temperature range. When CaO is used as the CO ₂ absorbent,
CaO + CO ₂ → CaCO ₃
CO ₂ is absorbed and removed by the absorbent according to the reaction of 1. By removing CO ₂ in the gasification gas in this way, the following shift reaction easily proceeds to the right.

CO + H ₂ O → CO ₂ + H ₂
In this state, the temperature raising oxygen or air is supplied to the upstream side of the reforming catalyst layer by the normal flow path of the oxygen or air supply line 19.
2) When the CO ₂ absorption amount reaches saturation, the oxygen or air used for raising the temperature of the catalyst packed bed during normal operation is switched to the oxygen or air supply line 19 to change the flow path of the CO ₂ absorbent packed bed. Directly upstream, the absorbent is heated to a temperature range of 800 to 950 ° C, preferably 850 to 900 ° C. In this temperature range, the carbonate of the CO ₂ absorbent is thermally decomposed and CO ₂ is desorbed from the same absorbent.

In the CO ₂ absorption / reformation furnace 4, the temperature rise due to the injection of oxygen or air is caused by the heat of oxidation reaction of tar components, H ₂ , CO, and CH ₄ .

When CO ₂ absorption amount of CO ₂ absorbent has reached the saturation, the value of the downstream CO ₂ analyzer 18 indicating the CO ₂ concentration of the gasification gas provided downstream of the high-temperature boiler 11 starts to rise, above As described above, the temperature-raising oxygen or air is supplied immediately upstream of the CO ₂ absorbent packed bed. When the absorbent is heated to a temperature range of 800 to 950 ° C., preferably 850 to 900 ° C., CaCO ₃ begins to decompose, and the generated CO ₂ flows downstream. At this time, the shift reaction is not promoted because the concentration of CO _{2 in} the gasification gas temporarily rises. Approaching the CO ₂ concentration indicated respectively by provided upstream of CO ₂ absorption and reformer 4 and upstream CO ₂ analyzer 17 indicating the CO ₂ concentration in the gasification gas and the downstream CO ₂ analyzer 18 Then, the flow of temperature-raising oxygen or air is returned to immediately upstream of the reforming catalyst layer, and the temperature of the catalyst packed bed is lowered to 450 to 700 ° C, preferably 540 to 640 ° C.

  After that, the above operations 1) and 2) are repeated.

By removing CO ₂ by the CO ₂ absorbent packed bed, the following shift reaction in the reforming catalyst packed bed can be promoted.

Assuming toluene as a typical example of tar, the main reactions that occur in the CO ₂ absorption / reforming furnace 4 are as follows.

i) C ₇ H ₈ + 9O ₂ → 7CO ₂ + 4H ₂ O ... Oxidation reaction
ii) C ₇ H ₈ + 7H ₂ O → 7CO + 11H ₂・ Reforming reaction
iii) CO + H ₂ O → CO ₂ + H ₂ ···· Shift reaction
iv) In addition, when oxygen is excessively present, an oxidation reaction of H ₂ , CO, CH _4, etc. also occurs.

Cooling Tower Treatment The high temperature gas of 850 to 900 ° C. that emerges from the bottom of the CO ₂ absorption / reforming furnace 4 is sent to the high temperature boiler 11 where it is subjected to heat recovery treatment, and then to the cooling tower 12 at a temperature of 170 to 180 ° C. Sent. Aqueous NaOH solution is circulated in the cooling tower 12, whereby CO ₂ in the gasification gas is absorbed and the generated Na ₂ CO ₃ salt is recovered and removed. Therefore, greenhouse gas is not emitted.

Power Generation Step The low temperature gas having a temperature of 55 to 60 ° C. that has exited the cooling tower 12 is sent to the power generation facility 5 equipped with a gas turbine and a gas engine, and used there for power generation.

Carrier gas The gas discharged from the power generation facility 5 at a temperature of 400 ° C. is then subjected to heat recovery treatment by the low temperature boiler 13, and then part of it is released to the atmosphere at 170 to 180 ° C., and the rest is dehumidified by the carrier gas line 9 in the dehumidifier 14 , The cyclone upstream side additive supply line 6 and the cyclone downstream side additive supply line 7 via the booster 15 and the tank 16 and are sent to respective starting ends of the cyclone upstream side additive supply line 7 and the carrier gas of the cyclone upstream side additive and the cyclone downstream side additive ( It is used as a gas temperature of 50 ° C. The oxygen concentration in this gas is about 1 to 2% by volume, and the injection ratio of the carrier gas to the outlet gas of the gasification furnace is 1/15 to 1/30. (LHV) does not decrease.

Experimental Example Next, an experimental example of the present invention will be shown.

An experiment was conducted by changing each condition in the system shown in FIG. 1 in which power is generated using a combustible gas obtained by gasifying and reforming waste. An example of the composition of the outlet gas of the gasification furnace 1 is shown in Table 1, the temperature of the gasification furnace 1 and the CO ₂ absorption / reforming furnace 4 and the air ratio to each outlet gas are shown in Table 2, and the desalination / desulfurization agent and The relationship between the desalination / desulfurization performance is shown in FIG. 2, the air ratio to the outlet gas of the power generation equipment 5 is shown in Table 3, the relationship between the desalination / desulfurization agent and the desalination / desulfurization performance is shown in Table 4 and FIG. Table 5 shows the results of thermodynamic equilibrium calculation regarding the generation and decomposition of (CaO + CO ₂ ⇔ CaCO ₃ ).

According to Table 5, in the CO ₂ absorption tower, the inlet CO ₂ is 8.1%, and at 600 ° C., 96.98% of CO ₂ is absorbed and removed by equilibrium calculation (at 650 ° C., 89.37). %). Further, when the temperature of the absorption tower is raised to 850 ° C., it will decompose until the outlet CO ₂ concentration becomes 38.59% (at 900 ° C., it will decompose to 79.48%).

Claims (10)

A gasification process for partial combustion gasification of a gasification material, a cyclone treatment process for collecting coarse powder of gasification gas emitted from the gasification process, and a coarse powder-removed gasification gas produced from the cyclone treatment process From the CO ₂ absorption / reformation step, and a CO ₂ absorption / reformation step of CO ₂ absorption / reformation processing of the dust-removed gasified gas discharged from the bag filter treatment step. In a gasification power generation system including a power generation process for generating power using reformed gas,
After the gasification step and before the cyclone treatment step, a cyclone upstream additive having a desalination / desulfurization function is used as an additive carrier gas after the heat recovery of the gas generated from the power generation step to produce a gasification gas. Supply to, and
The CO ₂ absorbing agent used in the CO ₂ absorbing and reforming process is CO ₂ absorbed in the temperature range of the gas temperature range 450-700 ° C., when the CO ₂ absorption amount reaches saturation, the reforming catalyst SoNoboru temperature The flow of oxygen or air is switched from immediately upstream of the reforming catalyst layer to immediately upstream of the CO ₂ absorbent packed bed, and the absorbent packed bed is heated to a temperature range of 800 to 950 ° C. to remove CO ₂ from the absorbent. Characterized by releasing the
A method for removing an acid component at high temperature in a gasification power generation method. The acid component removal method at high temperature in the gasification power generation method according to claim 1, wherein the cyclone upstream side additive also has a CO ₂ absorption / removal function.   The method for removing an acid component at a high temperature in the gasification power generation method according to claim 1 or 2, wherein the cyclone upstream additive has an average particle diameter of 100 to 1000 µm.   The cyclone upstream additive is selected from the group consisting of calcined dolomite, slaked lime, sodium aluminate and baking soda at high temperatures in the gasification power generation method according to any one of claims 1 to 3. Acid component removal method of.   A cyclone downstream additive which has a desalination / desulfurization function and may be the same as or different from the cyclone upstream additive after the cyclone treatment step and before the bag filter treatment step, , An additive selected from the group consisting of calcined dolomite, slaked lime, sodium aluminate and baking soda is used as an additive carrier gas after heat recovery of the gas generated from the power generation step, and is supplied to the gasification gas from which coarse powder has been removed. The method for removing an acid component at high temperature in the gasification power generation method according to any one of claims 1 to 4, which is characterized in that.   The crude powder containing the additive is collected in the cyclone treatment step, and the collected coarse powder is supplied to the gasification step together with the gasification material. A method for removing an acid component at a high temperature in the gasification power generation method according to any one of claims. Wherein the CO ₂ absorbing agent used in the CO ₂ absorbing reforming step is selected from the group consisting of CaO, Ca _{(OH) 2} and burnt dolomite, as claimed in any one of claims 1 to 6 A method for removing an acid component at high temperature in a gasification power generation method. The gasification according to any one of claims 1 to 7, wherein the reformed gas is subjected to CO ₂ absorption treatment with an aqueous NaOH solution after heat recovery treatment to recover and remove generated Na ₂ CO ₃ . A method for removing an acid component at high temperature in a power generation method. A gasification furnace for partial combustion gasification of the gasification material, a cyclone installed downstream of the gasification furnace for collecting coarse powder of the gasification gas emitted from the furnace, and installed downstream of the cyclone. a bag filter for dust removal processing exiting crude powder-removed gasification gas from here, the installed downstream of the bag filter dust removal has been gasified gas from here to process the CO ₂ absorbing reforming CO ₂ absorption and Kai A gasification power generation system including a quality furnace and a power generation facility installed downstream of the CO ₂ absorption / reformation furnace to generate electric power using a reformed gas discharged from the furnace,
A cyclone upstream additive supply line for supplying an additive having a desalination / desulfurization function is provided in the flow path from the gasification furnace to the cyclone, and the carrier gas line coming from the power generation facility is connected to the supply line. It is, from immediately upstream of the reforming catalyst layer to oxygen or air for reforming RoNoboru temperature when CO ₂ absorption immediately upstream of the CO ₂ absorption and reformer CO ₂ absorbent filler layer reaches saturation An oxygen or air supply line for switching immediately upstream of the CO ₂ absorbent packed bed is connected,
High temperature acid component removal device in gasification power generation system.
In the flow path from the cyclone to the bag filter, a cyclone downstream side additive supply line for supplying an additive having a desalination / desulfurization function is provided, and a carrier gas line coming from the power generation facility is connected to the supply line. Is characterized by
An acid component removing device at high temperature in the gasification power generation system according to claim 9.