KR101032178B1 - Gasification system for converting carbonaceous feedstock into synthesis gas and method thereof - Google Patents

Abstract

PURPOSE: A system for gasifying a carbonous raw material into synthetic gas and a gasifying method using the same are provided to simplify the system by continuous reform the raw material into synthetic gas. CONSTITUTION: A system for gasifying a carbonous raw material into synthetic gas includes a storing bat(10), a carbonizing bath(30), a hydrogen reformer(50), and a refining unit(60). A raw material continuous supplying unit(20) supplies overheated vapor to a raw material in order to obtain a moisture containing raw material. The carbonizing bath includes a first carbonizing unit(310) and a second carbonizing unit(320). The hydrogen reformer includes a separate heating unit and applies heat required for a reforming reaction.

Description

[0001] The present invention relates to a gasification system for reforming a carbonaceous feedstock into a syngas, and a gasification system using the same,

The present invention relates to a gasification system having a cracking furnace and an H ₂ reformer that enable pyrolysis. The present invention also includes a method of producing synthesis gas using the gasification system.

Due to geopolitical factors such as rising prices of fossil fuels, the demand for sustainable energy availability, and the instability of oil-producing countries, the regional ubiquity of fossil fuels, and climate change, a wide range of carbonaceous materials, called so-called feedstocks, There is a growing awareness of combustible syngas raw materials made from various materials made of organic materials. In addition, materials made of solid carbonaceous materials or organic materials are accompanied by additional difficulties in terms of difficulty in supplying, combustion control, and byproduct treatment, and the value of this type of energy source is gradually diminishing.

In this situation, it is being sought to convert raw materials to syngas and recycle it. Compared with syngas and fossil fuels, it is possible to produce electricity by using advanced gas fuels while significantly reducing carbon dioxide emissions. Not only is it easy to switch, it is easy to switch to biodiesel.

Moreover, the feedstock used in the synthesis gas production can recycle resources that can be continuously supplied by most organic or synthetic methods.

Currently, combustion pyrolysis is the most common method of producing syngas, which is a process in which a feedstock is dried and then passed through a kiln or batch, (tar) are also produced.

In addition, in the direct oxygen combustion method, the upper layer of the pyrolysis furnace is filled with gas, while the lower layer is slagged.

The synthesis gas production method according to the prior art is generally inefficient and takes into consideration not only the economic problem in consideration of the energy source used for producing the product but also the cost of the synthesis gas and the processing cost of the byproduct.

The present invention includes an on-line process for synthesizing various types of feedstock into a high purity synthesis gas through a gasification process and an H ₂ reforming process.

In the gasification process according to the present invention, a certain amount of feedstock is fed to a first cracking section pyrolyzed under the determined heating temperature and pressure conditions, where pyrolysis gas containing synthesis gas and byproduct molecules gas.

A certain amount of by-products generated by pyrolysis under a relatively high pressure in the first condensing section is transferred to the pyrolysis second condensing section. The impurities such as the male and tar constituting the by-product are converted into syngas through the second pyrolysis process, (ash) state.

Since the first and second portions are assembled so as to be able to communicate with each other, internal conditions of high temperature and high pressure are transferred to the second pyrolysis gas stream in the first pyrolysis unit, The high temperature and high pressure state can be maintained.

The pyrolysis gas produced in the _first condensing section is supplied to a reforming reactor (H ₂ reforming reactor) for H ₂ synthesis and is subjected to a reforming process by reacting with ionized water or superheated steam of high temperature and high pressure.

Also, the syngas produced in the second dry fraction is converted from the H ₂ reformer into the saturated syngas according to the quality of the synthesis gas.

In, the state 1 and / or 2, the dry distillation gas generated by the dry distillation unit is made of a saturated syngas with H ₂ synthesis in the H ₂ reformer, over at least one purification unit it clean (clean) as previously described do.

The final syngas thus purified can be used for alternative to natural gas fuels, for the production of biodiesel or for the manufacture of chemicals.

According to the present invention, the present invention is provided to convert a feedstock into a synthesis gas inexpensively and continuously on the basis of a gasification process for pyrolysis and an H ₂ reforming process.

Since the present invention is capable of producing a dry gas having a small content of impurities while being divided into two dry streams in one reactor and performing one or more thermal decomposition processes, it is possible to simplify the facilities and to continuously pyrolyze the dry gas in one reactor So that the production efficiency can be maximized.

The present invention reduces the adherent material (for example, alkali metal material, etc.) when reforming H ₂ , thereby prolonging the service life and operating condition of the facility.

When the purified syngas is generated, the energy required for the initial startup is cut off and the self-produced synthesis gas is converted into a self-contained mode by using the self-produced syngas as an energy source to increase the energy efficiency. It is designed to be recycled.

1 is a flow chart schematically illustrating the operation principle of the gasification system according to the present invention.
2 is a block diagram of a gasification system for producing syngas according to the present invention.
FIG. 3 is a block diagram illustrating the gasification system and the heat recovery system shown in FIG. 2 together.
4 is a view schematically showing a structure of a nebulizer installed in the system of the present invention.

Now, a system for reforming a carbonaceous feedstock according to the present invention into syngas and a method of operation thereof will be described in more detail with reference to the accompanying drawings.

Fig. 1 is a flow chart schematically illustrating the operation principle of a gasification system according to the present invention, and Fig. 2 is a block diagram of a gasification system for producing a syngas according to the present invention.

The gasification system with syngas according to the present invention is designed to reform syngas from various types of feedstock as described above and includes a reservoir 10, a reflux furnace 30, an H ₂ reformer 50 And a refining apparatus 60, and may preferably include a continuous feedstock supply apparatus 20, at least one dust collecting apparatus 40, and a plurality of heat exchangers.

The reservoir 10 provided in the system of the present invention is adapted to receive various types of feedstock to be modified into syngas and to guide them to the system of the present invention (SlOO), where the term " feedstock " Are used to produce biomass (eg, timber, rice straw, corn husks, palm husks), industrial and municipal waste, coal tar in steel mills, petroleum coke, (Carbonaceous feedstock) having a certain carbon conversion content such as a material, a low-grade fossil fuel, or the like.

The feedstock stored in the storage tank 10 is supplied to at least one feedstock continuous supply device 30 disposed upstream of the carbonization furnace 30 before being supplied to the carbonization furnace 30 which is pyrolyzed under an oxygen- A predetermined amount of the feedstock may be continuously supplied to the carbon monoxide reflux reactor 30 through the reactor 20 (S110). In addition, the continuous feedstock supply apparatus 20 is capable of pre-conditioning the physical characteristics required in the gasification and carburization process to be performed in the gasification furnace 30 to ensure a sound carbonization condition. To achieve this object, And an accumulation system.

The outside air cutoff device helps remove the air contained in the feedstock to be supplied to the carbonization furnace 30 and supply it to the carbonization furnace 30 in an oxygen-free state. In addition, the pressure balancing device may guide the supply amount of the feedstock to be supplied to the carbonization furnace 30 in a batch, that is, with a constant volume of the feedstock to the carbonization stream and simultaneously apply the pressure.

As described above, the feedstock continuous feeder 20 composed of the outside air cutoff device and the pressure balance device is provided in at least one manner, so that the feedstock processed in each feedstock continuous feeder 20 is continuously fed 30 so that the synthesis gas can be continuously produced.

In addition, the feedstock continuous feeder 20 provides superheated steam to the feedstock to contain a predetermined amount of moisture in the feedstock, which superheated steam is fed from the superheater 130 (see FIG. 3) Will be more specifically described.

Then, the feedstock to be continuously supplied at a constant pressure and volume is pyrolyzed in an anaerobic / non-combustion manner inside the carbonaceous furnace 30 to produce a carbonaceous gas (S200). The internal structure of the dry flow path 30 and the dry flow method therefor will be described in more detail with reference to FIG.

The gasification furnace 30 is composed of a first condensing part 310 and a second condensing part 320, and the first and second condensing parts 310 and 320 are partitioned to be mutually communicable. The dry furnace 30, like the continuous feedstock feeder, provides superheated steam to the feedstock to contain the desired moisture in the feedstock to induce the H ₂ reforming process, which is fed from the superheater. In addition, water is injected into the gasification chamber, and the mixing ratio of water and water is estimated to be in the range of about 1 to 2, and the mixing ratio of water is in the range of the constituent elements (C, H, O, N, S) Based on the content of carbon and hydrogen, the amount of water supplied is controllably controlled.

First is guided to a dry distillation unit 310 and / or the second dry distillation unit 320, the dry distillation gas is through one or more cyclones (40) (S230) H _2, the reformer 50 is produced subjected to H ₂ synthesis (S300). Some of the gaseous streams are similar to those of the syngas discharged at the final stage. These gaseous streams can bypass the H ₂ synthesis process and bypass the purification process. As is well known to those skilled in the art, the H ₂ synthesis process can produce a feed gas having a constant molecular ratio through contact with superheated steam.

The dust collecting device 40 prevents the byproducts (for example, ash) contained in the gasified gas discharged from the gasification furnace 30 (for example, ash) or undissolved solids from entering the subsequent process. If the undissolved solids If the subsequent process, that is introduced into the H ₂ reformer 50, it will typically require an additional excess heat to maintain the internal temperature of the H ₂ from the H ₂ required for the reformer reforming process. The undifferentiated solid matter collected in the dust collecting device 40 is recycled back to the gasification furnace 30 to produce the gasified gas through the gasification process, and the remaining by-products are discharged to the outside.

The H ₂ reformer 50 reacts with the ionized water or the superheated steam at a high temperature in order to produce syngas (or raw material gas) having a constant atomic ratio as described above, The dry gas that has undergone sufficient H ₂ reforming process is made of a saturated syngas with a high ratio of H ₂ / CO.

The H ₂ reformer 50 is provided separately with a reactor heating device (not shown) to provide a temperature required for the reforming reaction. Optionally, the reactor heating apparatus in the H ₂ reformer can use the syngas produced in the system of the present invention as a raw material. The H ₂ reformer 50 causes the dry gas and the superheated superheated steam to react with each other for a predetermined time (? _R ), wherein? _R may be within 10 seconds or 10 seconds or more, preferably 3 seconds? τ _R ≤ 7 seconds while controlling the amount of superheated steam injected to adjust the composition of the syngas to a predetermined value (H ₂ / CO ratio).

The syngas produced by the H ₂ reformer 50 is about 900 to 1,000 ° C. The syngas at a high temperature is passed through the heat exchanger 100 (see FIG. 3) disposed downstream of the H ₂ reformer and the refiner 60 Heat exchange with other medium can be performed, and the energy recovery rate of the present system can be improved.

The H ₂ reformer 50 is composed of multiple stages, preferably two or more stages, and is shown as a three stage stage reformer in FIG. For reference, the rate of H ₂ is also different because the difference between the residence time of the gaseous mixture produced by the first gaseous stream portion 310 and the gaseous stream produced by the second gaseous stream portion 320 is due to the difference in the residence time inside the gaseous stream. Therefore, in order to increase the proportion of H _2, the carbon monoxide gas produced in the first condensing portion 310 is guided into the first-stage reactor of the H ₂ reformer 50 to be discharged to the third-stage reactor, the dry distillation gas is guided to the H ₂ reformer 50 of the two-stage or three-stage reactor because of the high first dry distillation unit the ratio of H ₂ compared to the dry distillation gas discharged from the production. Since the dry gas discharged from the second dry portion 320 is generally composed of syngas, it is unnecessary to further perform the H ₂ reforming process and bypass the process to remove only the impurities contained in the dry gas It can be filtered and commercialized.

Then, the saturated syngas discharged from the H ₂ reformer 50 is recovered from the particulate matter, tar, other contaminants (for example, sulfur compounds, dissolved substances) contained in the syngas by means of the purifier 60 (S400).

FIG. 3 is a block diagram showing the gasification system and the heat recovery system shown in FIG. 2 together, and the solid arrows shown in FIG. 3 are diagrams showing a path modified by the synthesis gas through the gasification process of the feedstock, The dashed lines or thick dashed arrows illustrate the movement path of the heat source to be used in the system according to the invention. The gasification process of the feedstock indicated by the solid arrows has been fully described with reference to FIG. 2, and the detailed description thereof will be omitted here.

In the system according to the present invention, water can be supplied from the outside and converted into superheated steam necessary for each reactor and supplied.

The water to be supplied from the water source (not shown) is preferentially heated through the purification device 60, and the purification device 60 heats the high-temperature saturated synthetic gas produced in the H ₂ reformer 50 to relatively low- . The heated water is further heated through the first economizer 111 and the second economizer 112 and the waste heat boiler 120 and is saturated by means of a super heater 130 having a self- State superheated steam.

The first economizer 111 heats the water using the high-temperature combustion gas generated in the process of burning in the heating device of the H ₂ reformer 50 as a heat source. The combustion gas from the H ₂ reformer is supplied to the first economizer 111 to the waste heat boiler 120 and the waste heat boiler 120 is adapted to heat the hot water to be supplied through the first and / or the second economizer to a higher temperature do.

In addition, the second economizer 112 can use the high temperature combustion gas generated in the process of burning in the heating device of the superheater 130 as a heat source, thereby making the hot water into superheated steam.

In other words, the high-temperature combustion gas generated in the H ₂ reformer is discharged to the outside through the waste heat boiler 120 and the first economizer 111 while the high-temperature combustion gas generated in the superheater is discharged to the second economizer 112. And then discharged to the outside. Optionally, the first economizer and the second economizer may be monolithic.

The superheated steam in the saturated state heated by the superheater 130 is first supplied to the H ₂ reformer 50 while being supplied to the dry furnace 30 and the continuous feed material feeder 20.

The combustion air is required for the heating device for the H ₂ reformer 50 and the heating device for the superheater 130. In order to increase the temperature of the combustion air to be supplied to the heating device, And a heat exchanger (100) for inducing heat exchange between the hot saturated syngas produced in the H ₂ reformer.

In other words, the air for combustion is H ₂ reformer being from saturated synthesis gas at a high temperature produced in the 50 heat is conducted heat, and then H ₂ reformer is conducted from the combustion gas of high temperature generated from the 50 column again heated to And supplied to the heating device of the H ₂ reformer and the heating device of the superheater.

As described above, the system according to the present invention does not heat the combustion air and the superheated steam water through a separate combustion process but uses a variety of mediums of high temperature flowing in the system as a heat source to recover high temperature waste heat While each heating device is designed in a self-contained mode in which the self-synthesis gas produced in the system can be used as a raw material, while the synthesis gas is produced, except when the system of the present invention is initially operated have.

4 is a view schematically showing a structure of a nebulizer installed in the system of the present invention.

As shown in the figure, the dry cargo route 30 of the present invention is divided into a first carcass part 310 and a second carcass part 320, and the first carcass part 310 and the second carcass part 320 And can be opened and closed via the shut-off valve 330. [0064]

The first conveying unit 310 includes a supply pipe 311, a combustion furnace 312, a motor 313, a screw 314 disposed along the rotation axis of the motor 313, and a gas transfer pipe 315 The second conveying portion 320 includes a combustion furnace 322, a motor 323, a screw 324 disposed along the rotation axis of the motor 323, a gas transfer pipe 325, And a discharge pipe 326.

Preferably, the carbonaceous furnace 30 is surrounded by a water tube coil (not shown) for heat recovery on its outer surface and is sealed for contact protection so that heat radiation energy recovery and stability can be taken into consideration. The first and second condensed portions are surrounded by the refractory so as to withstand high temperatures around the combustion furnaces (312, 322).

The contents of the gasification furnace should be described more specifically through the gasification process to the gasification. First, the feedstock contained in the storage tank 10 (see FIG. 2) is introduced into the first condensing portion 310 of the carbonization furnace 30 through the supply pipe 311 of the first condensing portion 310. Then, the internal pressure (P ₁ ) and the temperature (T ₁ ) necessary for the feed of the feedstock are controlled and the residence time in the first dry portion, that is to say the thermal decomposition of the feedstock and the reaction time ₁ ). For reference, the internal pressure (P ₁ ), temperature (T ₁ ) and reaction time (△ τ ₁ ) are determined by pharmacodynamic calculation or experimentation of the feedstock.

Generally, the internal pressure (P ₁ ) is approximately 1.5 to 7.0 kg / cm 2, the temperature (T ₁ ) is approximately 500 to 1,000 ° C., and the reaction time (Δτ ₁ ) is 10 min ≦ Δτ ₁ ≦ 60 min.

The feedstock is progressively conveyed toward the shutoff valve 330 by means of the motor 313 and a screw 314 driven therewith under the internal conditions of the first dry portion 310. [ The internal temperature of the first condensing part 310 can be controlled by the indirect heating method by burning the syngas in the furnace 312 and the reaction time can be adjusted by the rotational speed of the screw 314 (S210).

During the anoxic and non-burning processes, the feedstock is separated into a dry gas and a solid material, and the dry gas is transferred to the downstream process along the gas transfer pipe 315, while the solid material is continuously passed through the secondary gasification process To the second gasifier 320 so as to perform the operation.

The solid material is injected into the second dry portion 320 having an internal condition similar to the first dry portion 310 through the open shutoff valve 330 so that the same gasification process as in the first dry portion 310 (S220). The reaction time △ τ ₂ can be controlled by adjusting the pressure P ₂ and the temperature T ₂ as described above by adjusting the internal temperature of the furnace 322 and controlling the reaction time with the rotation speed of the screw 324. [ . (T ₂ ) is about 500 to 1,000 ° C., the reaction time (Δτ ₂ ) is about 1.5 to 7.0 kg / cm ₂ , the internal pressure (P ₂ ) Is 3min ≤ ₂ ≤ 20min.

The solid material is pyrolyzed so that the dry gas is transferred to the downstream process along the gas transfer tube 325, while the solid discharge, i.e., the ashless carbon ash is discharged to the outflow conduit 30 through the discharge pipe 326.

Since the carbonaceous gas generated through the pyrolysis process in the carbonaceous furnace 30 is composed of syngas and other gaseous materials containing by-product molecules, a secondary gasification process such as the system of the present invention is required for producing a high quality fuel .

As the feedstock may be selected, the secondary gasification process may be omitted depending on the content of the fixed carbon. Since the feedstock with low fixed carbon content is not easy to be decomposed and gasified, the energy consumption is significantly increased. In this case, the supply of superheated steam or ionized water to each of the cargo passages in the first and second gasification stages Can be used to produce syngas at higher concentrations and good quality.

The dry gas to be transferred to the gas transfer tubes 315 and 325 is transported downstream to carry out the H ₂ reforming step via the superheated steam of high temperature for H ₂ synthesis.

It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.

10 ----- Storage tank,
20 ----- Feedstock continuous feeder,
30 ----- With the current,
40 ----- Dust collector,
50 ----- H ₂ reformer,
60 ----- Purification device,
100 ----- Heat exchanger,
111,112 ----- Economizer,
120 ----- Waste heat boiler,
130 ----- Super heater.

Claims (17)

A storage tank (10) for storing a feedstock;
(30) capable of pyrolyzing the feedstock in an oxygen-free and indirect heating manner;
A multi-stage H ₂ reformer (50) having a self-heating device for bringing the carbonized gas produced in the gasification furnace (30) into contact with the superheated steam to produce H ₂ ;
A purifier 60 for removing impurities contained in the synthesis gas produced by the H ₂ reformer 50; And
And a super heater (130) having a self heating device to supply the moisture required for the H ₂ reformer (50) in the superheated steam state,
The gasification furnace 30 includes a supply pipe 311 for supplying the feedstock, a combustion furnace 312 for providing an internal heat source, a motor 313 disposed outside, A first condensing part 310 having a screw 314 disposed thereon and a gas transfer tube 315 for guiding the pyrolyzed gas to the H ₂ reformer 50;
A combustion chamber 322 for providing an internal heat source, a motor 323 disposed outside, a screw 324 disposed around the rotation axis of the motor 323, a gas delivery pipe (325) for discharging byproducts, and a discharge pipe (326) for discharging byproducts; And
And a shutoff valve 330 disposed between the first and second dryers 310 and 320 to divide the first and second dryers 310 and 320. The first and second dryers 310 and 310 And the second carbonization unit 320 are connected to each other so as to perform the indirect thermal decomposition process. The gasification system reforms carbonaceous feedstock into synthesis gas.
delete The method of claim 1, wherein the internal pressure of the dry distillation to 1 (310) (P ₁₎ was 1.5 ~ 7.0kg / ㎠, temperature (T ₁₎ is 500 ~ 1,000 ℃, the reaction time (△ τ ₁₎ is ≤ 10min Gt; 60 min. ≪ / _RTI >
2. The method according to claim 1, wherein the internal pressure P ₂ of the second dry portion 320 is 1.5 to 7.0 kg / cm 2, the temperature T ₂ is 500 to 1,000 ° C., and the reaction time Δτ ₂ is 3 min ≤ △ τ ₂ ≤ 20 min.
The method according to claim 1, characterized in that at least one continuous feedstock supply device (20) for continuously supplying the feedstock to the continuous-flow furnace (30) at a constant volume is added between the storage tank (10) Wherein the gasification system comprises:
The gasification system of claim 1, wherein the H ₂ reformer (50) comprises two or more stages of reactors.
The method of claim 1, wherein the H ₂ reformer 50, the heater and the waste heat boiler 120 and the at least one economizer for recovering high-temperature combustion gas waste heat to the heating device of the super heater 130, and the H ₂ reformer Further comprising a heat exchanger (100) for recovering heat from the hot syngas produced in the gasification system (50).
The gasification system of claim 1, further comprising at least one dust collecting device (40) downstream of the first and second dryers (310, 320).
Supplying the feedstock to the carbonization furnace 30 (S100);
A step (S200) of pyrolyzing the feedstock in an oxygen-free / indirect-heating manner at a high temperature and a high pressure in the gasification furnace (30) to gasify the carbonized gas;
A step (S300) of reforming H ₂ by contacting the carbonized gas with a high-temperature superheated steam to synthesize the carbon dioxide with a synthesis gas;
Purifying the syngas (S400); And
A method of gasification comprising reforming a carbonaceous feedstock into syngas, comprising the step of supplying superheated steam made in the superheater (130) to the gasification step (S200) or the H ₂ reforming step (S300).
10. The method of claim 9, further comprising continuously and uniformly supplying (S110) the feedstock continuously and continuously through at least one feedstock continuous feeder (20) disposed upstream of the feedstream Way.
The gasification system according to claim 9, wherein the gasification furnace (30) comprises a first gasification unit (310) and a second gasification unit (320) And a second gasification step (S220) carried out in the second gasification section (320).
10. The method of claim 9, comprising the step of collecting (S230) various types of solid matter contained in the dry gas, downstream of the gasifying step (S200).
12. The method according to claim 11, wherein the various types of solid matter collected in the dust collecting step (S230) are guided to the gas flow path (30).
The gasification method according to claim 9, comprising recovering the heat released from the high-temperature syngas produced in the H ₂ reforming step (S300) to the heat exchanger (100).
10. The method of claim 9, comprising recovering heat from the hot saturated syngas in the syngas purification step (S400).
The gasification method according to claim 9 or 10, wherein the superheated steam generated by the heating of the superheater (130) is supplied to the feedstock continuous supply step (S110).
The method of claim 9 or claim 16, further comprising the steps of: recovering the hot combustion gas generated in the combustion process of the H ₂ reforming step (S300) to the waste heat boiler (120) And recycling the hot combustion gas generated in the heat exchanger to an economizer.

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