CN113184805A - Comprehensive utilization and carbon fixation process for pyrolysis gas - Google Patents
Comprehensive utilization and carbon fixation process for pyrolysis gas Download PDFInfo
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Abstract
The application discloses a pyrolysis coal gas comprehensive utilization and carbon sequestration process, belongs to the technical field of pyrolysis coal gas utilization, and can solve the problem that the existing utilization of pyrolysis coal gas can cause environmental pollution. The process comprises the following steps: carrying out pressure swing adsorption on the pyrolysis coal gas to extract hydrogen to obtain desorption gas; carrying out fine desulfurization and fine deoxygenation treatment on the desorbed gas to obtain primary treated gas; converting methane and carbon monoxide in the primary treatment gas to obtain hydrogen and carbon dioxide, and obtaining secondary treatment gas; separating nitrogen, hydrogen and carbon dioxide from the secondary treatment gas by pressure swing adsorption decarburization to obtain synthesis gas and carbon dioxide gas; conveying the synthesis gas to an ammonia synthesis device to synthesize liquid ammonia; and synthesizing the urea from the carbon dioxide gas and the liquid ammonia. The method realizes the high-efficiency utilization of pyrolysis coal gas by quality classification, simultaneously realizes the purpose of carbon fixation, basically realizes zero carbon emission in the technical process, and has great significance for carbon emission reduction.
Description
Technical Field
The application relates to the technical field of pyrolysis coal gas utilization, in particular to a comprehensive pyrolysis coal gas utilization and carbon sequestration process.
Background
Coal is a main energy source in China and is also a high-carbon energy source. At present, most areas in northern China frequently encounter haze weather, coal becomes popular while the blue-day guard war makes a sound, and clean and efficient utilization of the coal is listed as an important special science and technology item. Over the years, practices in various places show that part of suitable coal is graded and graded to be converted into oil, gas, electricity and clean coal, so that gradient utilization is realized, and clean and efficient utilization of the coal can be realized while the main energy status of the coal is kept. In the process of the coal briquette quality-classified clean utilization, byproduct pyrolysis coal gas is generated, and the pyrolysis coal gas mainly contains hydrogen, carbon monoxide, carbon dioxide, nitrogen, oxygen, hydrogen sulfide and the like.
At present, most of pyrolysis gas is burnt as power generation fuel, and a small part of pyrolysis gas is converted to extract hydrogen and then is used as coal tar to be hydrogenated to prepare fuel oil for use. At present, the utilization of pyrolysis gas, whether the pyrolysis gas is used as power generation fuel to be burnt or used as fuel oil, can generate a large amount of carbon-containing waste gas and cause environmental pollution.
Disclosure of Invention
The embodiment of the application can solve the problem that the existing pyrolysis coal gas utilization causes environmental pollution by providing the pyrolysis coal gas comprehensive utilization and carbon sequestration process.
The embodiment of the invention provides a pyrolysis gas comprehensive utilization and carbon fixation process, which comprises the following steps:
carrying out pressure swing adsorption on the pyrolysis coal gas to extract hydrogen to obtain desorption gas;
carrying out fine desulfurization and fine deoxygenation treatment on the desorbed gas to obtain primary treated gas;
performing conversion treatment on methane and carbon monoxide in the primary treatment gas to obtain hydrogen and carbon dioxide, and obtaining secondary treatment gas;
separating nitrogen, hydrogen and carbon dioxide from the secondary treatment gas through pressure swing adsorption decarburization to obtain synthesis gas and carbon dioxide gas;
conveying the synthesis gas to an ammonia synthesis device to synthesize liquid ammonia;
and synthesizing urea from the carbon dioxide gas and the liquid ammonia.
In a possible implementation manner, the step of subjecting the pyrolysis coal gas to pressure swing adsorption to extract hydrogen to obtain desorption gas further comprises the steps of:
and mixing hydrogen obtained by extracting hydrogen from the pyrolysis coal gas through pressure swing adsorption with coal tar to prepare fuel oil.
In a possible implementation manner, the delivering the synthesis gas to the ammonia synthesis plant for synthesizing liquid ammonia further includes the steps of:
and conveying the external hydrogen to the ammonia synthesis device.
In a possible implementation manner, the external hydrogen is obtained by extracting hydrogen from the pyrolysis coal gas through pressure swing adsorption.
In a possible implementation manner, the adsorbents used for separating nitrogen, hydrogen and carbon dioxide from the secondary treatment gas by pressure swing adsorption decarburization to obtain synthesis gas and carbon dioxide gas include activated carbon, molecular sieves and cuprous chloride loaded adsorbents.
In a possible implementation manner, the pressure swing adsorption decarburization of the secondary treatment gas to separate nitrogen, hydrogen and carbon dioxide by pressure swing adsorption decarburization to obtain synthesis gas and carbon dioxide gas comprises the following steps: adsorption, pressure equalizing and reducing, reverse releasing, vacuumizing and boosting.
In a possible implementation manner, before the desorption gas is subjected to the fine desulfurization and fine deoxygenation treatment to obtain the primary treatment gas, the method further comprises the following steps:
and boosting the desorption gas to a preset pressure value.
In a possible implementation, the preset pressure value is greater than 0.6 MPa.
In a possible implementation manner, the step of subjecting the pyrolysis gas to pressure swing adsorption to extract hydrogen to obtain desorbed gas specifically includes the steps of:
and carrying out desalting treatment, pretreatment, concentration treatment, deoxidation treatment and purification treatment on the pyrolysis coal gas, and then extracting hydrogen to obtain desorption gas.
In one possible implementation, the concentration process and the purification process each include the following steps: adsorption, three-time pressure equalizing and reducing, reverse discharging, vacuumizing, pre-boosting, three-time pressure equalizing and boosting and final product boosting.
One or more technical solutions provided in the embodiments of the present invention have at least the following technical effects or advantages:
the embodiment of the invention provides a pyrolysis gas comprehensive utilization and carbon fixation process, which comprises the following steps: carrying out pressure swing adsorption on the pyrolysis coal gas to extract hydrogen to obtain desorption gas; carrying out fine desulfurization and fine deoxygenation treatment on the desorbed gas to obtain primary treated gas; converting methane and carbon monoxide in the primary treatment gas to obtain hydrogen and carbon dioxide, and obtaining secondary treatment gas; separating nitrogen, hydrogen and carbon dioxide from the secondary treatment gas by pressure swing adsorption decarburization to obtain synthesis gas and carbon dioxide gas; conveying the synthesis gas to an ammonia synthesis device to synthesize liquid ammonia; and synthesizing the urea from the carbon dioxide gas and the liquid ammonia. According to the comprehensive utilization and carbon fixation process for the pyrolysis gas, the carbon-containing gas and the liquid ammonia are finally synthesized into the urea, so that the purpose of classifying and efficiently utilizing the pyrolysis gas according to the quality is realized, the carbon fixation purpose is realized, zero carbon emission in the process is basically realized, the significance for carbon emission reduction is great, and the environmental pollution is greatly reduced.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the description of the embodiments of the present invention will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
FIG. 1 is a flow chart of a pyrolysis gas comprehensive utilization and carbon sequestration process provided by an embodiment of the present application;
FIG. 2 is a schematic structural diagram of a pyrolysis gas comprehensive utilization and carbon sequestration system provided in an embodiment of the present application;
fig. 3 is a schematic structural diagram of a pressure swing adsorption hydrogen extraction device provided in an embodiment of the present application.
Icon: 1-a pressure swing adsorption hydrogen extraction device; 11-a desalination plant; 12-a pre-treatment device; 13-a concentration device; 14-hydrogen production and deoxidation device; 15-a purification device; 2-a desulfurization unit; 3-a deoxygenation device; 4-a transformation device; 5-pressure swing adsorption decarbonization device; 6-an ammonia synthesis plant; 7-urea synthesis unit; 8-fuel oil preparation facilities.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the embodiments of the present invention, it should be noted that the terms "primary", "secondary", and "tertiary" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. Furthermore, the terms "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. Specific meanings of the above terms in the embodiments of the present invention can be understood by those of ordinary skill in the art according to specific situations.
Coal is a main energy source in China and is also a high-carbon energy source. At present, most areas in the north of China frequently encounter haze weather, and the weather is protected in the blue skyWhen the defense fight is played, coal becomes popular, and clean and efficient utilization of coal is listed as an important special science and technology item. Over the years, practices in various places show that part of suitable coal is graded and graded to be converted into oil, gas, electricity and clean coal, so that gradient utilization is realized, and clean and efficient utilization of the coal can be realized while the main energy status of the coal is kept. The coal briquette can generate a byproduct of pyrolysis coal gas in the process of quality-based, grading, cleaning and utilizing, wherein the pyrolysis coal gas mainly contains hydrogen (chemical formula: H)2) Carbon monoxide (chemical formula: CO), carbon dioxide (chemical formula: CO 22) Nitrogen (chemical formula: n is a radical of2) Oxygen (chemical formula: o is2) Hydrogen sulfide (chemical formula: h2S), and the like.
At present, most of pyrolysis gas is burnt as power generation fuel, and a small part of pyrolysis gas is converted to extract hydrogen and then is used as coal tar to be hydrogenated to prepare fuel oil for use. At present, the utilization of pyrolysis gas, whether the pyrolysis gas is used as power generation fuel to be burnt or used as fuel oil, can generate a large amount of carbon-containing waste gas and cause environmental pollution.
In view of the above problems, an embodiment of the present application provides a pyrolysis gas comprehensive utilization and carbon sequestration process, as shown in fig. 1, including the following steps 101 to 106:
step 101: and (3) carrying out pressure swing adsorption on the pyrolysis coal gas to extract hydrogen to obtain desorption gas. This step is typically carried out in a pressure swing adsorption hydrogen extraction unit 1, as shown in figure 2.
The pyrolysis coal gas is a byproduct generated in the coal quality grading, cleaning and utilizing process, and is a coal gas containing dust. The pyrolysis gas comprises the following components in percentage by weight as shown in table 1:
TABLE 1 composition and content of pyrolysis gas
| Component (A) | N2 | H2 | CO | CH4 | CO2 | H2S | O2 | CmHn |
| Content (V%) | 43～48 | 25～27 | 10～13 | 6～9 | 7 | 5～6 | 0.4～1.0 | 1～2 |
In practical application, step 101: the method comprises the following steps of (1) carrying out pressure swing adsorption on pyrolysis coal gas to extract hydrogen to obtain desorption gas, and specifically comprises the following steps: and (3) carrying out desalting treatment, pretreatment, concentration treatment, deoxidation treatment and purification treatment on the pyrolysis coal gas, and then extracting hydrogen to obtain desorption gas.
As shown in fig. 3, the desalination treatment is generally carried out in a desalination device 11, the desalination device 11 comprising a washing column, the output of which communicates with the input of the pre-treatment device 12. The specific process of the desalting treatment of the desalting device 11 is as follows: the pyrolysis gas discharged from the pyrolysis furnace is compressed by a compressor and then enters washingAt the bottom of the tower, pyrolysis gas enters the upper end of the washing tower after fully contacting with the filler and the circulating liquid at the lower part of the washing tower, is discharged from the top of the tower after being subjected to high-efficiency desalted water spray washing, and enters the pretreatment after passing through a gas-liquid separator. More than 90% of ammonia and ammonium salt can be removed from the pyrolysis gas through desalting treatment; after the pyrolysis coal gas is washed, the tar content is about 200mg/Nm3Naphthalene content of about 50mg/Nm3。
As shown in fig. 3, the pretreatment is generally carried out in a pretreatment device 12, and the pretreatment device 12 includes a pretreatment column, an input port of which is communicated with the demineralization device 11, and an output port of which is communicated with an input port of the concentration device 13. The pretreatment device 12 is used for the pretreatment process, wherein the desalted and washed pyrolysis gas enters the pretreatment tower from the bottom of the pretreatment tower to remove water, tar and naphthalene. The tar content of the pretreated pyrolysis gas is less than or equal to 3mg/Nm3, and the naphthalene content is less than or equal to 5mg/Nm 3. And the pretreated pyrolysis gas is sent to a concentration device 13 for concentration treatment. Wherein, the regeneration gas that the preliminary treatment produced is carried to the boiler for the electricity generation to further make full use of the composition in the pyrolysis coal gas, rationally utilized the energy.
As shown in fig. 3, the concentration treatment and the deoxidation treatment are generally performed in the concentration device 13 and the hydrogen production and deoxidation device 14. The concentration device 13 comprises four adsorption towers, the input port of the first adsorption tower is communicated with the output port of the pretreatment device 12, the output port of the last adsorption tower is communicated with the input port of the hydrogen production and deoxidation device 14, and the specific processes of concentration treatment and deoxidation treatment are as follows: the concentration treatment of the concentration device 13 adopts a 12-4-3-1 process, and the four adsorption towers are always in a feeding adsorption state, and the process comprises the following steps: adsorption, three-time pressure equalizing and reducing, reverse discharging, vacuumizing, pre-boosting, three-time pressure equalizing and boosting and final product boosting. The hydrogen production and deoxidation device 14 comprises a deoxidation tower, an input port of the deoxidation tower is communicated with an output port of the concentration device 13, an output port of the deoxidation tower is communicated with an input port of the purification device 15, concentrated hydrogen with the hydrogen content of more than 45% -50% is obtained after concentration treatment, the concentrated hydrogen enters the deoxidation tower for deoxidation after heating, and the concentrated hydrogen is sent to purification treatment after cooling gas-liquid separation.
As shown in fig. 3, the purification process is generally performed in a purification apparatus 15, the purification apparatus 15 includes four adsorption towers which are sequentially connected, an input port of the first adsorption tower is connected to an output port of the hydrogen production and deoxidation apparatus 14, a first output port of the last adsorption tower is connected to an input port of the desulfurization apparatus 2, and a second output port is respectively connected to the fuel oil preparation apparatus 8 and the ammonia synthesis apparatus 6. The purification device 15 has the following specific purification process, wherein four adsorption towers are used in the purification process, a 12-4-3-1 process is adopted, and the four adsorption towers are always in a feeding adsorption state, and the process comprises the following steps: adsorption, three-time pressure equalizing and reducing, reverse discharging, vacuumizing, pre-boosting, three-time pressure equalizing and boosting and final product boosting. Purified hydrogen with the hydrogen content of more than 99.9 percent is obtained after purification treatment. Wherein, the cis-bleed gas of purification treatment is carried to the pre-pressure step of concentration treatment to can the rational utilization energy, reduction in production cost. Wherein, the low calorific value desorption gas that purification treatment produced is carried to the boiler for the electricity generation, has realized making full use of the low calorific value desorption gas that purification treatment produced.
In addition, the concentration device 13 may be communicated with a pyrolysis furnace so that desorption gas with a higher calorific value generated by concentration treatment is conveyed to the pyrolysis furnace, and heat generated by combustion can be used for pyrolysis of coal. The concentration device 13 can also be communicated with a boiler, so that desorption gas with higher heat value generated by concentration treatment is conveyed to the boiler and can be used for power generation. The concentration device 13 is respectively communicated with the pyrolysis furnace and the boiler, so that the high-calorific-value desorption gas generated by concentration treatment is fully utilized.
The components of the desorbed gas after pressure swing adsorption hydrogen extraction are shown in table 2:
TABLE 2 composition and content of desorbed gas
| Component (A) | N2 | H2 | CO | CH4 | CO2 | H2S | O2 |
| Content (V%) | 70～75 | 6.5 | 10.5 | 2.5 | 7 | 5～6 | 0.4～1.0 |
Step 102: and carrying out fine desulfurization and fine deoxygenation treatment on the desorbed gas to obtain primary treated gas.
The hydrogen sulfide and the oxygen in the purified desorption gas can be removed through fine desulfurization and fine deoxygenation treatment, so that the subsequent poisoning of the adsorbent by the hydrogen sulfide is avoided. As shown in FIG. 2, the fine desulfurization treatment is performed in the desulfurization device 2, the fine deoxygenation is performed in the deoxygenation device 3, the input port of the desulfurization device 2 is communicated with the output port of the pressure swing adsorption hydrogen extraction device 1, the output port is communicated with the input port of the deoxygenation device 3, and the output port of the deoxygenation device 3 is communicated with the input port of the shift device 4. And after the desorption gas is subjected to fine desulfurization and fine deoxygenation treatment, the primary treatment gas at the moment contains nitrogen, hydrogen, carbon dioxide, carbon monoxide and methane.
Step 103: and (3) converting methane and carbon monoxide in the primary treatment gas to obtain hydrogen and carbon dioxide, and obtaining secondary treatment gas.
Step 103 specifically includes converting methane into carbon monoxide and hydrogen through shift conversion, and converting carbon monoxide in the carbon monoxide and primary process gas into hydrogen and carbon dioxide through shift conversion. The transformation process involves the following chemical reaction equation:
CH4+H2O→CO+3H2
CO+H2O→H2+CO2
the secondary treatment gas after the transformation treatment comprises nitrogen, hydrogen and carbon dioxide, the transformation process is simple and convenient, five gases can be converted into three gases through the transformation treatment, and the three gases are the existing gases in the original desorption gas and other additional gases cannot be added. As shown in FIG. 2, the shift treatment is carried out in the shift converter 4, and the input port of the shift converter 4 is connected to the output port of the deoxidation apparatus 3, and the output port is connected to the input port of the pressure swing adsorption decarburization apparatus 5.
Step 104: and (3) separating nitrogen, hydrogen and carbon dioxide from the secondary treatment gas by pressure swing adsorption decarburization to obtain synthesis gas and carbon dioxide gas. As shown in FIG. 2, the pressure swing adsorption decarburization is carried out in a pressure swing adsorption decarburization device 5, the input port of the pressure swing adsorption decarburization device 5 is communicated with the shift device 4, and the output port is communicated with the input port of the ammonia synthesis device 6 and the input port of the urea synthesis device 7, respectively.
Specifically, the pressure swing adsorption decarbonization device 5 contains an adsorbent, and the adsorbent can adsorb carbon dioxide in secondary treatment gas, so that nitrogen, hydrogen and carbon dioxide gas are separated, the nitrogen and the hydrogen are mixed into synthesis gas, and then the adsorbent is desorbed to obtain the carbon dioxide gas. Because the synthesis gas is used for synthesizing liquid ammonia in the synthesis ammonia device 6 subsequently, the carbon dioxide is separated from the nitrogen and the hydrogen in the step, and the carbon dioxide can be prevented from being mixed into the synthesis gas to cause the poisoning of a catalyst used when the synthesis gas is used for synthesizing the liquid ammonia.
The adsorbent can make active components adhere to the particle surface, is a solid substance capable of effectively adsorbing some components from gas or liquid, has large specific surface area, proper pore structure and surface structure, has strong adsorption capacity on the adsorbent, generally does not react with the adsorbent and a medium, is convenient to manufacture and easy to regenerate, and has excellent adsorbability.
The adsorbent used for performing pressure swing adsorption on the purified desorbed gas provided by the embodiment of the invention comprises activated carbon, a molecular sieve and a cuprous chloride loaded adsorbent.
The active carbon is prepared by carbonizing and activating carbon-containing raw materials such as charcoal, fruit shells, coal and the like. The activated carbon has huge specific surface area and abundant pore structures, and the specific surface area can reach 500-1700 m2Wherein the small pore volume is generally 0.15 ml/g-0.9 ml/g, the surface area accounts for more than 95% of the specific surface area, the transition pore volume is generally 0.02 ml/g-0.1 ml/g, the large pore volume is generally 0.2 ml/g-0.5 ml/g, the surface area is very small and is only 0.5 m/g2/g～2m2And/g, so that the activated carbon has excellent adsorption performance.
The molecular sieve is an artificially synthesized hydrated aluminosilicate (zeolite) or natural zeolite with molecular sieving effect, and has chemical formula of M2M)O·Al2O3·xSiO2·yH2O, M', M are each a monovalent or divalent cation, e.g. K+、Na+、Ca2 +、Ba2+Etc., x is SiO2The number of moles, also known as the Al/Si ratio, y represents the number of moles of water. The molecular sieve has many pore passages with uniform pore diameter and regularly arranged holes, and the molecular sieves with different pore diameters separate molecules with different sizes and shapes. The molecular sieve has the advantages of high adsorption capacity, strong selectivity and high temperature resistance.
The cuprous chloride supported adsorbent has a strong adsorption effect on carbon dioxide molecules, but has a weak adsorption effect on nitrogen and hydrogen molecules, and carbon dioxide in the secondary treatment gas can be greatly removed by using the cuprous chloride supported adsorbent. The cuprous chloride supported adsorbent in the embodiment of the invention is a molecular sieve loaded with cuprous chloride. For example, chlorineThe cuprous oxide supported adsorbent can be prepared by mixing CuCl and gamma-Al2O3And 4A, 13X, NaY, Cu+And (3) mixing and heating the molecular sieves such as the Y grade and the like respectively to obtain the adsorbent.
Further, the pressure swing adsorption decarburization in step 104 comprises the following steps: adsorption, pressure equalizing and reducing, reverse releasing, vacuumizing and boosting.
Step 105: the synthesis gas is conveyed to an ammonia synthesis device 6 to synthesize liquid ammonia.
The total content of hydrogen and nitrogen in the synthesis gas accounts for 99.99 percent (volume fraction) of the synthesis gas, the synthesis gas is conveyed to an ammonia synthesis device 6 to synthesize liquid ammonia, an input port of the ammonia synthesis device 6 is communicated with an output port of a pressure swing adsorption decarburization 5 device, an output port is communicated with an input port of a urea synthesis device 7, and the chemical reaction formula in the synthesis gas is as follows:
N2+3H2＝2NH3
because the synthesis gas at this moment has more nitrogen and less hydrogen content, a large amount of nitrogen is left after the synthesis gas is directly used for synthesizing the liquid ammonia, so that the waste of the nitrogen is caused, and the purity of the liquid ammonia is lower. In order to avoid the waste of nitrogen and the low purity of liquid ammonia, the synthesis gas is conveyed to the synthesis ammonia device 6 for synthesizing liquid ammonia, and the method further comprises the following steps: and (3) conveying the external hydrogen to the ammonia synthesis device 6, so that the ratio of the nitrogen to the hydrogen after the hydrogen is supplemented is 3: and (1) synthesizing ammonia, so that nitrogen in the synthesis gas can be fully utilized, and the purity of the liquid ammonia is greatly improved. The external hydrogen can be obtained by extracting hydrogen from pyrolysis coal gas through pressure swing adsorption, so that the hydrogen generated after the hydrogen is extracted from the raw coal gas can be effectively utilized, and meanwhile, the production cost can be reduced.
Step 106: and synthesizing the urea from the carbon dioxide gas and the liquid ammonia.
Wherein the chemical reaction formula of the synthetic urea is as follows:
2NH3+CO2＝CO(NH2)2+H2O
the carbon-containing gas in the pyrolysis gas is finally converted into the carbon dioxide, and the carbon dioxide and the liquid ammonia synthesize the urea, so that zero carbon emission of the pyrolysis gas is realized, the environmental pollution is greatly reduced, the carbon dioxide gas for synthesizing the urea is converted from the carbon-containing gas of the pyrolysis gas, the pyrolysis gas is fully utilized, the carbon dioxide gas does not need to be additionally added from the outside, the resources are effectively utilized, and the production cost is reduced.
In practical application, the pyrolysis coal gas is subjected to pressure swing adsorption to extract hydrogen to obtain desorption gas, and the method further comprises the following steps: the fuel oil is prepared by mixing the hydrogen obtained by extracting hydrogen from the pyrolysis gas through pressure swing adsorption and the coal tar, so that the hydrogen obtained by pyrolyzing the gas can be effectively utilized, and the pyrolysis gas is more fully utilized. As shown in figure 2, hydrogen obtained by extracting hydrogen from pyrolysis gas through pressure swing adsorption and coal tar are mixed to prepare fuel oil in a fuel oil preparation device 8, an input port of the fuel oil preparation device 8 is communicated with a second output port of the pressure swing adsorption hydrogen extraction device 1, and the fuel oil preparation device 8 comprises a reactor.
Specifically, the hydrogen and coal tar are mixed in a ratio of 900-1000: 1, then feeding the mixture into a reactor, and reacting at 350-370 deg.C under 5-10 MPa at a space velocity of 1 hr-1～3h-1The components are 4 wt% -6 wt% of CoO and 15 wt% -20 wt% of MoO3、15wt％～25wt％WO3The balance being nano Al2O3(the particle diameter is 5-20 nm) under the action of a catalyst of a carrier, and liquid products are obtained through gas-liquid separation to obtain the fuel oil.
Step 102: before the desorption gas is subjected to fine desulfurization and fine deoxygenation treatment to obtain primary treatment gas, the method further comprises the following steps: and (5) boosting the desorption gas to a preset pressure value. Specifically, the desorption gas is pressurized to a preset pressure value and is carried out in a pressure boosting device, an input port of the pressure boosting device is communicated with a first output port of the pressure swing adsorption hydrogen extraction device 1, and an output port of the pressure boosting device is communicated with the desulfurization device 2 and is used for boosting the desorption gas to the preset pressure value.
The pressure of the desorption gas obtained by pressure swing adsorption hydrogen extraction of the strong pyrolysis gas is small (about 0.2 MPa-0.3 Mp), and the pressure of the desorption gas reaches a preset pressure value through pressure boosting, so that the subsequent process can be conveniently and better carried out. The preset pressure value is associated with the subsequent fine desulfurization and fine deoxygenation treatment. For example, the preset pressure value may be set to be greater than 0.6 MPa.
The embodiment of the invention provides a pyrolysis gas comprehensive utilization and carbon fixation process, which comprises the following steps: carrying out pressure swing adsorption on the pyrolysis coal gas to extract hydrogen to obtain desorption gas; carrying out fine desulfurization and fine deoxygenation treatment on the desorbed gas to obtain primary treated gas; converting methane and carbon monoxide in the primary treatment gas to obtain hydrogen and carbon dioxide, and obtaining secondary treatment gas; separating nitrogen, hydrogen and carbon dioxide from the secondary treatment gas by pressure swing adsorption decarburization to obtain synthesis gas and carbon dioxide gas; the synthesis gas is conveyed to a synthesis ammonia device 6 to synthesize liquid ammonia; and synthesizing the urea from the carbon dioxide gas and the liquid ammonia. According to the comprehensive utilization and carbon fixation process for the pyrolysis gas, the carbon-containing gas and the liquid ammonia are finally synthesized into the urea, so that the purpose of classifying and efficiently utilizing the pyrolysis gas according to the quality is realized, the carbon fixation purpose is realized, zero carbon emission in the process is basically realized, the significance for carbon emission reduction is great, and the environmental pollution is greatly reduced.
The embodiments in the present specification are described in a progressive manner, and the same or similar parts among the embodiments may be referred to each other, and each embodiment focuses on the differences from the other embodiments.
The above embodiments are only used to illustrate the technical solutions of the present application, and not to limit the present application; although the present application has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications or substitutions do not depart from the spirit and scope of the present disclosure.
Claims (10)
1. A pyrolysis gas comprehensive utilization and carbon sequestration process is characterized by comprising the following steps:
carrying out pressure swing adsorption on the pyrolysis coal gas to extract hydrogen to obtain desorption gas;
carrying out fine desulfurization and fine deoxygenation treatment on the desorbed gas to obtain primary treated gas;
performing conversion treatment on methane and carbon monoxide in the primary treatment gas to obtain hydrogen and carbon dioxide, and obtaining secondary treatment gas;
separating nitrogen, hydrogen and carbon dioxide from the secondary treatment gas through pressure swing adsorption decarburization to obtain synthesis gas and carbon dioxide gas;
conveying the synthesis gas to an ammonia synthesis device to synthesize liquid ammonia;
and synthesizing urea from the carbon dioxide gas and the liquid ammonia.
2. The pyrolysis gas comprehensive utilization and carbon sequestration process according to claim 1, wherein the pyrolysis gas is subjected to pressure swing adsorption hydrogen extraction to obtain desorbed gas, and further comprising the steps of:
and mixing hydrogen obtained by extracting hydrogen from the pyrolysis coal gas through pressure swing adsorption with coal tar to prepare fuel oil.
3. The comprehensive utilization and carbon sequestration process for pyrolysis gas as claimed in claim 1, wherein the step of delivering the synthesis gas to an ammonia synthesis device for synthesis of liquid ammonia further comprises the steps of:
and conveying the external hydrogen to the ammonia synthesis device.
4. The comprehensive utilization and carbon sequestration process for pyrolysis gas as claimed in claim 3, wherein the external hydrogen is obtained by pressure swing adsorption of hydrogen from the pyrolysis gas.
5. The comprehensive utilization and carbon sequestration process for pyrolysis gas as claimed in claim 1, wherein the secondary treatment gas is subjected to pressure swing adsorption decarbonization to separate nitrogen, hydrogen and carbon dioxide, and the adsorbents used for obtaining the synthesis gas and the carbon dioxide gas comprise activated carbon, molecular sieves and cuprous chloride loaded adsorbents.
6. The comprehensive utilization and carbon sequestration process for pyrolysis gas as claimed in claim 1 or 5, wherein the pressure swing adsorption decarbonization for separating nitrogen, hydrogen and carbon dioxide from the secondary treatment gas to obtain synthesis gas and carbon dioxide gas comprises the following steps: adsorption, pressure equalizing and reducing, reverse releasing, vacuumizing and boosting.
7. The comprehensive utilization and carbon sequestration process for pyrolysis gas as claimed in claim 1, wherein before the desorption gas is subjected to fine desulfurization and fine deoxygenation treatment to obtain a primary treated gas, the process further comprises the steps of:
and boosting the desorption gas to a preset pressure value.
8. The comprehensive utilization and carbon sequestration process for pyrolysis gas as claimed in claim 7, wherein the preset pressure value is greater than 0.6 MPa.
9. The pyrolysis gas comprehensive utilization and carbon sequestration process according to claim 1, wherein the desorption gas is obtained by subjecting the pyrolysis gas to pressure swing adsorption hydrogen extraction, and the process specifically comprises the steps of:
and carrying out desalting treatment, pretreatment, concentration treatment, deoxidation treatment and purification treatment on the pyrolysis coal gas, and then extracting hydrogen to obtain desorption gas.
10. The comprehensive utilization and carbon sequestration process for pyrolysis gas as claimed in claim 9, wherein the concentration treatment and the purification treatment both comprise the following steps: adsorption, three-time pressure equalizing and reducing, reverse discharging, vacuumizing, pre-boosting, three-time pressure equalizing and boosting and final product boosting.
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