KR101160769B1 - Apparatus and method for recovering carbon dioxide and hydrogen of high purity using waste - Google Patents

Abstract

An apparatus and method are provided for recovering carbon dioxide and hydrogen without installing a separate compressor by boosting a synthetic gas of atmospheric pressure generated from plasma gasified waste using a high pressure blower and an ejector.

Description

Carbon dioxide and hydrogen recovery apparatus using waste and method thereof {APPARATUS AND METHOD FOR RECOVERING CARBON DIOXIDE AND HYDROGEN OF HIGH PURITY USING WASTE}

The present invention relates to an apparatus for recovering carbon dioxide and hydrogen using waste, and more particularly, to recovering high-purity carbon dioxide and hydrogen from atmospheric pressure synthesis gas generated by gasifying waste, biomass, coke or coal. An apparatus and method are provided.

Waste generated daily in homes, offices and workplaces is a social issue for environmental and economic reasons. In the past, waste has been disposed of by landfill or incineration. However, landfilling waste not only causes environmental pollution due to the generation of leachate and gas, but also costs a lot of landfills and landfill facilities.

Incineration of waste also requires a system for lowering atmospheric hazardous substances (eg dioxin, furan, volatile organic compounds, etc.) generated during incineration, and a separate method for treating harmful ashes. .

As an alternative to landfill or incineration of waste, techniques have been developed for plasma pyrolysis and gasification of waste to generate syngas and recover carbon dioxide and hydrogen used as energy resources from the syngas. This technology is not just environmentally friendly to waste disposal, it adds value in that it recovers energy resources from waste. However, carbon dioxide and hydrogen must be recovered with high purity in order to be used as an energy source. This carbon dioxide and hydrogen recovery technology is equally applicable to gasification of biomass, petroleum coke and coal, as well as silk waste.

In order to solve the above problems, the present invention, in order to separate and recover the carbon dioxide and hydrogen from the atmospheric pressure synthesis gas generated by plasma pyrolysis / gasification without compressing to more than 10 atmospheres necessary for hydrogen recovery from the first stage with a large-capacity compressor By using a high pressure blower, an ejector, and a low capacity compressor, the present invention provides a device and a method for reducing power consumption and separating and recovering carbon dioxide and hydrogen with high efficiency.

In addition, the present invention can simplify the configuration of the device by recovering carbon dioxide and generating residual hydrogen-rich gas using a three-bed carbon dioxide PSA, a device that can recover the carbon dioxide by performing a single reduced pressure equilibrium operation And to provide a method.

The present invention provides a first knockout drum for removing water from a synthetic gas at atmospheric pressure generated by gasification of waste gas, a high pressure blower for firstly boosting the moisture-removed synthesis gas, and the first boosted synthesis gas. A desulfurizer, a first guard bed to remove fine dust from the desulfurized syngas, a preheater to preheat the syngas from which the fine dust has been removed, an ejector to secondary boost the preheated syngas, and an internal space to fill A high temperature water gas shift (WGS) reactor for producing carbon dioxide and hydrogen by reacting the iron-chromium-based catalyst and steam with carbon monoxide contained in the secondary boosted synthesis gas, and syngas discharged from the high temperature WGS reactor A heat exchanger for cooling, a second guard bed for removing sulfur and chlorine from the primary cooled synthesis gas, a copper-zinc catalyst filled in the interior space A low temperature water gas shift (WGS) reactor for reducing the concentration of carbon monoxide contained in the synthesis gas discharged from the second guard bed by using a cooler for secondarily cooling the synthesis gas discharged from the low temperature WGS reactor using cooling water; A second knockout drum for removing moisture from the secondary cooled synthesis gas, a carbon dioxide pressure swing adsorption (PSA) that recovers carbon dioxide from the moisture-depleted synthesis gas and generates a residual hydrogen rich gas, and a residual produced from the carbon dioxide PSA Provided is a carbon dioxide and hydrogen recovery apparatus including a compressor for compressing a hydrogen rich gas and hydrogen pressure swing adsorption (PSA) for recovering the compressed residual hydrogen rich gas to high purity hydrogen.

The carbon dioxide and hydrogen recovery apparatus according to the present invention boosts the synthesis gas of atmospheric pressure generated from the waste by plasma pyrolysis / gasification step by step using a high pressure blower, an ejector, and a compressor, thus eliminating the need to install a large-capacity compressor from the beginning. Energy savings and the ability to operate the carbon dioxide PSA at a pressure range appropriate for the carbon dioxide separation efficiency can improve recovery efficiency.

In addition, the configuration and the process of the apparatus can be simplified by configuring three or less carbon dioxide PSAs and performing only one pressure reduction equilibrium operation of the synthesis gas for recovering carbon dioxide.

1 is a view showing a carbon dioxide and hydrogen recovery system according to an embodiment of the present invention.
2 is a view showing the configuration of carbon dioxide PSA according to an embodiment of the present invention.
3 is a flowchart illustrating a carbon dioxide and hydrogen recovery method according to an embodiment of the present invention.

BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, embodiments of the present invention will be described with reference to the accompanying drawings. In the following description of the present invention, detailed description of known functions and configurations incorporated herein will be omitted when it may make the subject matter of the present invention rather unclear. Terminology used herein is a term used to properly express a preferred embodiment of the present invention, which may vary according to a user, an operator's intention, or a custom in the field to which the present invention belongs. Therefore, the definitions of the terms should be made based on the contents throughout the specification.

1 is a view showing a carbon dioxide and hydrogen recovery system according to an embodiment of the present invention. The carbon dioxide and hydrogen recovery system shown in FIG. 1 largely includes a waste gasifier 100 and a carbon dioxide and hydrogen recovery apparatus 200.

In order to recover carbon dioxide and hydrogen from the waste, a waste gasifier 100 for gasifying the waste is required. The waste gasifier 100 is a device for generating a synthesis gas by gasifying waste, and may include a synthesis gas generating device and a purification device.

The waste gasifier 100 is a waste input device 110 for gasifying waste, a plasma melting furnace 120, a waste heat boiler 130 connected to a rear end of the plasma melting furnace 120, and a bag filter connected to a rear end of the waste heat boiler 130. Filter 140 and wet scrubber 150.

The plasma melting furnace 120 receives the compressed waste from the waste input device 110. In addition, the plasma melting furnace 120 gasifies the injected waste using oxygen and a plasma jet generated from the plasma torch. Specifically, the waste is rapidly oxidized or gasified with oxygen by a high temperature plasma jet at 10,000 ° C., and ash or metals contained in the waste are melted in the plasma melting furnace 120. As a result of this melting, slag and synthesis gas are produced.

The slag is discharged through the slag outlet 121 provided in the plasma melting furnace 120, the synthesis gas is discharged to the waste heat boiler 130.

The waste heat boiler 130 recovers the heat of the synthesis gas, cools it, and discharges it to the bag filter 140.

The bag filter 140 removes fugitive dust included in the cooled syngas, and the wet scrubber 150 cleans the acid gas contained in the syngas.

In addition, the wet scrubber 150 discharges the synthesis gas from which the acidic gas has been cleaned to the carbon dioxide and hydrogen recovery device 200. In this case, the washed syngas is discharged at atmospheric pressure. Synthetic gas discharged from the wet scrubber 150 includes hydrogen (H ₂ ), carbon monoxide (CO), carbon dioxide (CO ₂ ), water (H ₂ O) and nitrogen (N ₂ ).

On the other hand, the carbon dioxide and hydrogen recovery device 200 is a device for recovering carbon dioxide and hydrogen from the synthesis gas.

Conventional carbon dioxide recovery apparatus (not shown) maintained the PSA operating pressure at 100 to 500 psi (about 7 to 34.5 barg) to separate and recover carbon dioxide and hydrogen from the synthesis gas. As such, in order to maintain a high operating pressure of 100 psi or more, the carbon dioxide recovery apparatus must include a compressor for boosting the synthesis gas to high pressure. However, compressors for boosting synthesis gas to high pressure are expensive equipment, and the power demand is high, which increases the manufacturing and operating costs of the system.

In addition, the conventional carbon dioxide recovery apparatus requires at least five beds, which adds to the cost of installing the beds and piping connected to each bed. In addition, the carbon dioxide recovery apparatus requires a plurality of pressure reduction equilibrium operations for decompressing the syngas boosted to a high pressure at least five times, which complicates the configuration and the process of the apparatus.

Carbon dioxide and hydrogen recovery device 200 according to an embodiment of the present invention does not require a compressor for boosting the synthesis gas of the atmospheric pressure to a high pressure at a time, and has three beds in the carbon dioxide recovery device, the reduced pressure equilibrium It is configured in the form of reduced operation.

Referring to FIG. 1, the carbon dioxide and hydrogen recovery apparatus 200 includes a buffer tank 201, a first knockout drum 202, a high pressure blower 210, a desulfurizer 220, and a first guard bed 230. ), Preheater 231, ejector 240, high temperature water gas shift (WGS) reactor 250, heat exchanger 251, second guard bed 260, low temperature water gas shift (WGS) reactor 270, A cooler 271, a second knockout drum 272, carbon dioxide Pressurized Swing Adsorption (PSA) 280, a compressor 286, and hydrogen Pressurized Swing Adsorption (PSA) 290.

The buffer tank 201 stores the syngas at atmospheric pressure discharged from the waste gasifier 100, and discharges the syngas at atmospheric pressure to the first knock out drum 202.

The first knockout drum 202 is connected to the buffer tank 201 and removes moisture from the synthesis gas at atmospheric pressure. The synthetic gas at atmospheric pressure discharged from the waste gasifier 100 may contain about 10% of moisture, and the first knockout drum 202 extracts and removes the moisture.

A high pressure blower 210 is connected to the first knockout drum 202 and firstly boosts the moisture-removed syngas to a pressure of 1.0 to 1.5 barg (about 15 to 20 psi).

The desulfurizer 220 desulfurizes the synthesis gas primarily boosted by the high pressure blower 210. The primary boosted synthesis gas contains about several ppm of sulfur, and the sulfur content of the synthesis gas can be reduced to 1 ppm or less by desulfurizing the synthesis gas. The removal of the sulfur component is to prevent the copper-zinc-based catalyst charged in the internal space of the low temperature WGS reactor 270 from being damaged by the sulfur component.

The first guard bed 230 is a silica guard bed, which is connected to the rear end of the desulfurizer 220 and removes fine dust when a sulfur-free synthetic gas is injected. In addition, the preheater 231 preheats the synthesis gas from which the fine dust is removed from the first guard bed 230 to about 350 ° C.

The ejector 240 supplies about 10 barg of steam to secondaryly boost the preheated syngas to 2.0 to 3.0 barg. The ejector 240 must supply steam having a weight and volume of three times the weight and volume of the injected synthesis gas. However, according to the combination of the boost operation with the high pressure blower 210 which processes the primary boost of the synthesis gas, the ejector 240 may reduce and supply the weight and volume of steam to 1 to 2 times the synthesis gas.

Specifically, the high temperature WGS reactor 250 connected to the rear end of the ejector 240 requires three times the steam compared to the molar ratio of the carbon monoxide concentration in the synthesis gas. This can be an amount (weight and volume) of steam corresponding to 1 to 1.5 times the total synthesis gas. Therefore, the ejector 240 may supply 1 to 2 times the steam in relation to the weight and volume of the total synthesis gas and discharge it to the high temperature WGS reactor 250. In this case, since it is difficult to increase the pressure of the synthesis gas to 2.0 to 3.0 barg at the discharge end by using the ejector 240 alone, the high pressure blower 210 is provided to increase the first pressure to 1 to 1.5 barg.

The high pressure blower 210 and the ejector 240 are inexpensive compared to the compressor and have a low power demand, and thus can perform the pressure boosting process of the synthesis gas more economically and efficiently.

The high temperature WGS reactor 250 is filled with an iron-chromium catalyst in the internal space, and supplies steam during the reaction. Thus, the high temperature WGS reactor 250 reacts the iron-chromium catalyst and steam with carbon monoxide contained in the secondary boosted synthesis gas to produce carbon dioxide and hydrogen. In this case, the high temperature WGS reactor 250 may set the operating temperature during the reaction to 350 to 450 ° C.

In addition, the high temperature WGS reactor 250 can produce a large amount of carbon monoxide as carbon dioxide and hydrogen by rapidly reacting carbon monoxide and steam by the iron-chromium catalyst, the concentration of carbon monoxide at the outlet side of the thermal equilibrium is about 4% As high as Accordingly, the synthesis gas is passed through the heat exchanger 251, the second guard bed 260, and the low temperature WGS reactor 270 connected to the rear end of the high temperature WGS reactor 250 to reduce the concentration of carbon monoxide to 1% or less.

In detail, the heat exchanger 251 first cools the synthesis gas discharged from the high temperature WGS reactor 250. Accordingly, the synthesis gas heated to a temperature of 350 to 450 ℃ in the high temperature WGS reactor 250 can be dropped to a temperature of 180 to 200 ℃. Before the primary cooled syngas is sent to the low temperature WGS reactor 270, the sulfur and chlorine components are removed using a second guard bed 260 connected to the heat exchanger 251.

The desulfurization treatment of the synthesis gas through the desulfurization unit 220, but the copper-zinc-based catalyst filled in the internal space of the low-temperature WGS reactor 270 is very susceptible to sulfur and chlorine components, the second guard bed 260 Sulfur and chlorine are removed through the process.

The second guard bed 260 is a hydrogen sulfide / hydrogen chloride guard bed, and the inner space may be filled with the same or similar catalyst as the copper-zinc catalyst filled in the low temperature WGS reactor 270. Accordingly, the second guard bed 260 reacts the sulfur component and the chlorine component included in the synthesis gas with the catalyst to reduce the sulfur component and the chlorine component included in the synthesis gas to 0.1 ppm or less.

The low temperature WGS reactor 270 reacts with the synthesis gas using a copper-zinc-based catalyst packed in the internal space, thereby reducing the concentration of carbon monoxide contained in the synthesis gas discharged from the second guard bed 260 to 1% or less. Let's do it.

The cooler 271 secondly cools the syngas discharged from the low temperature WGS reactor 270 using the coolant so that the syngas is at room temperature.

The second knockout drum 272 removes moisture (ie, condensate) condensed on the synthesis gas while the synthesis gas is secondarily cooled by the cooling water.

The carbon dioxide PSA 280 recovers carbon dioxide from the synthesis gas dehumidified in the second knockout drum 272 and generates residual hydrogen gas. The carbon dioxide PSA 280 includes three beds and a vacuum pump. The three beds and the vacuum pump desorb and recover carbon dioxide from the synthesis gas while the synthesis gas is passed and produce hydrogen rich gas. The carbon dioxide PSA 280 may recover more than 80% of carbon dioxide from the synthesis gas. At this time, the recovered carbon dioxide may have a high purity of 95% or more.

The carbon dioxide PSA 280 may also produce residual hydrogen gas from the synthesis gas, where the residual hydrogen gas is a residual hydrogen rich gas with 80% hydrogen content. In order to recover this residual hydrogen rich gas with 99.999% high purity hydrogen, carbon dioxide PSA 280 discharges the residual hydrogen rich gas to a compressor 286 connected to the rear stage.

The compressor 286 compresses the residual hydrogen rich gas to have a pressure of 10 to 15 barg.

Hydrogen PSA 290 recovers the compressed residual hydrogen rich gas with 99.999% high purity hydrogen. The hydrogen PSA 290 discharges impurities such as carbon monoxide and nitrogen, except for high purity hydrogen, to the off gas tank.

The carbon dioxide and hydrogen recovery apparatus 200 shown in FIG. 1 does not compress the synthesis gas of atmospheric pressure discharged from the waste gasifier 100 to a high pressure of 100 to 500 psi, and the high pressure blower 210 and the ejector 240. Primary and secondary boost to have pressures of 1.0 to 1.5 barg (about 15 to 20 psi) and 2.0 to 3.0 barg (about 30 to 40 psi). Therefore, there is no need to install a compressor for compressing the atmospheric synthesis gas to a high pressure of 100 to 500 psi.

The waste gasifier 100 shown in FIG. 1 shows a general configuration and may be a device that operates independently of the carbon dioxide and hydrogen recovery apparatus 200. Therefore, the waste gasifier 100 is not limited to the configuration shown in FIG. 1, and a waste gasifier having a different configuration may be applied.

In addition, in FIG. 1, only the contents of separating and recovering carbon dioxide and hydrogen from the synthesis gas generated by gasifying the waste are described. However, the waste gasifier 100 and the carbon dioxide and hydrogen recovery apparatus 200 may include biomass, coke or coal in addition to the waste. It is possible to separate and recover carbon dioxide and hydrogen from the synthesis gas produced by gasifying etc.

2 is a view showing the configuration of carbon dioxide PSA according to an embodiment of the present invention. Referring to FIG. 2, the carbon dioxide PSA 280 includes first to third beds 281, 282, and 283 and a vacuum pump 284, through which the carbon dioxide is recovered from the synthesis gas and the residual hydrogen gas. Create

The first to third beds 281, 282, and 283 each include an activated carbon-zeolitic catalyst filled in an internal space.

The vacuum pump 284 is connected to valves of the first to third beds 281, 282, and 283 to operate the inner spaces of the first to third beds 281, 282, and 283 in a vacuum state.

The first to third beds 281, 282, and 283 are composed of adsorption (ADS), reduced pressure equilibrium (E1D: Equalization), vacuum regeneration (V / V: Vac / Vent), elevated pressure equilibrium (E1R: Re-Pressurization) And boosting (F / P: Feed / Pressurization) operation.

In addition, the first to third beds 281, 282, and 283 may operate in the first, second, and third steps, and each step may include a first, second, and third sections. . The first to third beds 281, 282, and 283 may perform different operations for each section.

Hereinafter, an operation of the first to third beds 281, 282, and 283 in the first to third sections included in the first to third steps will be described in detail with reference to Table 1.

First step Step 2 3rd step Section 1 Second section Section 3 Section 1 Second section Section 3 Section 1 Second section Section 3 First bed absorption
(ADS) absorption
(ADS) Decompression equilibrium
(E1D) vacuum
play
(V / V) vacuum
play
(V / V) Boost equilibrium
(E1R) Waiting
(HOLD) Boost
(F / P) Boost
(F / P) 2nd bed Waiting
(HOLD) Boost
(F / P) Boost
(F / P) absorption
(ADS) absorption
(ADS) Decompression equilibrium
(E1D) vacuum
play
(V / V) vacuum
play
(V / V) Boost equilibrium
(E1R) 3rd bed vacuum
play
(V / V) vacuum
play
(V / V) Boost equilibrium
(E1R) Waiting
(HOLD) Boost
(F / P) Boost
(F / P) absorption
(ADS) absorption
(ADS) Decompression equilibrium
(E1D)

First, referring to Table 1, the first bed 281 performs the adsorption operation in the first section and the second section of the first step. Specifically, when synthesis gas is injected into the first bed 281, the first bed 281 adsorbs carbon dioxide contained in the synthesis gas using an activated carbon-zeolitic catalyst as an adsorbent during the first and second sections. The adsorption operation can be performed. The first bed 281 may have an operating pressure of about 1.0 to 2.5 barg during the adsorption operation.

Thereafter, the first bed 281 performs the decompression equilibrium operation in the third section of the first step. That is, in order to desorb the carbon dioxide adsorbed during the first section and the second section from the first bed 281, the first bed 281 depressurizes the internal pressure and maintains the depressurization equilibrium.

The first bed 281 performs a vacuum regeneration operation by operating the vacuum pump 284 in the first section and the second section of the second step, thereby discharging the carbon dioxide desorbed from the first bed 281 to the outlet 285. Recover through discharge.

Thereafter, the first bed 281 performs the step-up balance operation in the third section of the second step. That is, the first bed 281 boosts the internal pressure, and maintains the elevated pressure in equilibrium.

Meanwhile, the first bed 281 performs the standby operation in the first section of the third step and then performs the boosting operation in the second section and the third section of the third step. That is, the first bed 281 performs the preparation operation for adsorbing carbon dioxide from the synthesis gas injected into the first bed 281 by increasing the internal pressure again. When the third section of the third step is completed, the first bed 281 may repeat the operation according to each section included in the first to third steps again.

The operation of the second bed 282 and the third bed 283 is different from that of the first bed 281 in each of the sections included in the first to third steps. Carbon dioxide may be recovered by performing (E1D: Equalization), vacuum regeneration (V / V: Vac / Vent), boost equilibration (E1R: Re-Pressurization), and boosting (F / P: Feed / Pressurization) operations.

The carbon dioxide recovered through the first to third beds 281, 282, and 283 is discharged through the outlet 285. At this time, the carbon dioxide has a recovery rate of 80% or more and is recovered with high purity of 95% or more.

Although not shown through the drawings, in the case of using additional purification means and compression means, it is possible to recover with 99.99% carbon dioxide gas that can be used industrially or edible.

The carbon dioxide PSA 280 shown in FIG. 2 may recover high purity carbon dioxide using three beds and generate residual hydrogen gas. In addition, each of the beds 281, 282, and 283 performs one depressurization balance operation during the first to third steps, and does not perform a separate purge step or rinse step, thereby simplifying the operation.

3 is a flowchart illustrating a carbon dioxide and hydrogen recovery method according to an embodiment of the present invention. The carbon dioxide and hydrogen recovery method illustrated in FIG. 3 may be performed by the carbon dioxide and hydrogen recovery apparatus 200 illustrated in FIG. 1. The carbon dioxide and hydrogen recovery device 200 stores the synthetic gas discharged from the waste gasifier 100 in the buffer tank 201, and passes the synthesis gas through the first knockout drum 202 to remove moisture. .

The carbon dioxide and hydrogen recovery apparatus 200 firstly boosts the moisture-removed synthesis gas to 1.0 to 1.5 barg (step 310). Primary boosting of the syngas is performed by a high pressure blower 210. In addition, fine dust and sulfur components may be removed from the primary boosted synthesis gas.

Thereafter, the carbon dioxide and hydrogen recovery apparatus 200 preheats the synthesis gas to 350 ° C. (320). Then, the preheated synthesis gas is secondarily boosted to 2.0 to 3.0 barg (step 330).

On the other hand, the carbon dioxide and hydrogen recovery apparatus 200 reacts the carbon monoxide contained in the secondary boosted synthesis gas, steam (step 340). Specifically, the secondary boosted synthesis gas is injected into the high temperature WGS reactor 250 to produce carbon dioxide and hydrogen by reacting the iron-chromium catalyst and steam with carbon monoxide contained in the secondary boosted synthesis gas. In this case, the high temperature WGS reactor 250 sets the operating temperature during the reaction to 350 to 450 ° C. Therefore, the synthesis gas having completed the reaction may be first cooled using the heat exchanger 251.

Next, the carbon dioxide and hydrogen recovery apparatus 200 removes sulfur and chlorine from the synthesis gas (step 350). Since the sulfur and chlorine components damage the catalyst charged in the low temperature WGS reactor 270, these components are removed through the second guard bed 260 to reduce to less than 0.1 ppm.

In addition, the carbon dioxide and hydrogen recovery apparatus 200 reduces the concentration of carbon monoxide to 1% or less by reacting the synthesis gas and steam using a catalyst charged in the low temperature WGS reactor 270 (step 360). The synthesis gas discharged from the low temperature WGS reactor 270 is cooled to room temperature. It also removes the water (ie condensate) condensed on the synthesis gas while cooling.

Thereafter, the carbon dioxide and hydrogen recovery apparatus 200 recovers carbon dioxide from the synthesis gas and generates residual hydrogen gas (step 370). This step is performed in the carbon dioxide PSA 280, by desorbing and recovering carbon dioxide from the synthesis gas by driving three beds and a vacuum pump, to produce residual hydrogen gas.

Then, the carbon dioxide and hydrogen recovery apparatus 200 compresses the residual hydrogen gas (step 380), and recovers the hydrogen with high purity (step 390).

As described above, the present invention has been described by way of limited embodiments and drawings, but the present invention is not limited to the above embodiments, and those skilled in the art to which the present invention pertains various modifications and variations from such descriptions. This is possible.

Therefore, the scope of the present invention should not be limited to the described embodiments, but should be determined by the equivalents of the claims, as well as the claims.

100 waste gasifier 200 carbon dioxide and hydrogen recovery device
201: buffer tank 202: first knockout drum
210: high pressure blower 220: desulfurizer
230: first guard bed 231: preheater
240: ejector 250: high temperature WGS reactor
251 heat exchanger 260 second guard bed
270: low temperature WGS reactor 271: chiller
272: second guard bed 280: carbon dioxide PSA
281: first bed 282: second bed
283: third bed 284: vacuum pump
285 outlet 286 compressor
290 hydrogen PSA

Claims (7)

A first knockout drum for removing moisture from the atmospheric pressure synthesis gas generated by gasifying the waste;
A high pressure blower for first boosting the moisture-removed syngas;
A desulfurizer for desulfurizing the primary boosted synthesis gas;
A first guard bed for removing fine dust from the desulfurized synthesis gas;
A preheater for preheating the synthesis gas from which the fine dust has been removed;
An ejector for secondary boosting the preheated syngas;
A high temperature water gas shift (WGS) reactor for generating carbon dioxide and hydrogen by reacting the iron-chromium-based catalyst and steam filled in the internal space with carbon monoxide contained in the secondary boosted synthesis gas;
A heat exchanger for primary cooling the synthesis gas discharged from the high temperature WGS reactor;
A second guard bed for removing sulfur and chlorine from the primary cooled syngas;
A low temperature water gas shift (WGS) reactor for reducing the concentration of carbon monoxide contained in the synthesis gas discharged from the second guard bed by using a copper-zinc catalyst filled in the inner space;
A cooler for secondarily cooling the synthesis gas discharged from the low temperature WGS reactor using cooling water;
A second knockout drum for removing moisture from the secondary cooled syngas;
CO2 pressure swing adsorption (PSA) for recovering carbon dioxide from the water-removed synthesis gas and producing residual hydrogen rich gas;
A compressor for compressing the residual hydrogen rich gas produced in the carbon dioxide PSA; And
Hydrogen pressure swing adsorption (PSA) to recover the compressed residual hydrogen rich gas to high purity hydrogen
Carbon dioxide and hydrogen recovery device comprising a.
The method of claim 1,
The high pressure blower,
Carbon dioxide and hydrogen recovery apparatus for firstly boosting the moisture-removed atmospheric pressure synthesis gas to a pressure of 1.0 to 1.5 Barg.
The method of claim 1,
The ejector,
The preheated synthesis gas has a pressure of 8 to 12 barg, and supplies steam having a weight and volume of 0.5 to 2 times the weight and volume of the preheated synthesis gas to provide 2.0 to 3.0 barg of synthesis gas. A carbon dioxide and hydrogen recovery device for secondary pressure boosting.
The method of claim 1,
The carbon dioxide PSA,
3 beds; And
Vacuum pump connected to the three beds via piping
Carbon dioxide and hydrogen recovery apparatus comprising a.
The method of claim 4, wherein
Each of the three beds,
Activated carbon-zeolite catalyst is filled in the inner space
A carbon dioxide and hydrogen recovery apparatus for desorbing and recovering carbon dioxide from the moisture-removed syngas by the vacuum pump operated during operation and regeneration.
The method of claim 4, wherein
Each of the three beds,
And a carbon dioxide and hydrogen recovery apparatus for desorbing and recovering the moisture-containing synthetic gas through an adsorption operation, a reduced pressure balance operation, a vacuum regeneration operation, a boost balance operation, and a boost operation.
Removing moisture from the atmospheric synthesis gas produced by gasifying the waste;
Firstly boosting the moisture-removed syngas using a high pressure blower;
Desulfurizing the primary boosted syngas;
Removing fine dust from the desulfurized synthesis gas;
Preheating the synthesis gas from which the fine dust has been removed;
Secondly boosting the preheated syngas using an ejector;
Reacting the iron-chromium catalyst and steam charged in the internal space of a high temperature water gas shift (WGS) reactor with carbon monoxide contained in the secondary boosted synthesis gas to generate carbon dioxide and hydrogen;
Primary cooling the syngas discharged from the hot WGS reactor;
Removing sulfur and chlorine from the primary cooled syngas;
Reducing the concentration of carbon monoxide contained in the synthesis gas from which the sulfur component and the chlorine component are removed by using a copper-zinc-based catalyst packed in an internal space of a low temperature water gas shift (WGS) reactor;
Secondary cooling the syngas discharged from the low temperature WGS reactor using cooling water;
Removing moisture from the secondary cooled syngas;
Passing the moisture-depleted synthesis gas through carbon dioxide pressure swing adsorption (PSA) to recover carbon dioxide and generate residual hydrogen rich gas;
Compressing the residual hydrogen rich gas produced in the carbon dioxide PSA; And
Recovering the compressed residual hydrogen rich gas to the high purity hydrogen through hydrogen pressure swing adsorption (PSA)
Carbon dioxide and hydrogen recovery method comprising a.

Images