CN117866672A - Coke oven gas purifying system - Google Patents
Coke oven gas purifying system Download PDFInfo
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- CN117866672A CN117866672A CN202311729054.7A CN202311729054A CN117866672A CN 117866672 A CN117866672 A CN 117866672A CN 202311729054 A CN202311729054 A CN 202311729054A CN 117866672 A CN117866672 A CN 117866672A
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- 239000000571 coke Substances 0.000 title claims abstract description 43
- 239000007789 gas Substances 0.000 claims abstract description 156
- 238000001179 sorption measurement Methods 0.000 claims abstract description 65
- 239000012535 impurity Substances 0.000 claims abstract description 59
- 238000000034 method Methods 0.000 claims abstract description 51
- 238000000746 purification Methods 0.000 claims abstract description 40
- 230000008569 process Effects 0.000 claims abstract description 36
- 238000000926 separation method Methods 0.000 claims abstract description 34
- 230000006835 compression Effects 0.000 claims abstract description 30
- 238000007906 compression Methods 0.000 claims abstract description 30
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims abstract description 28
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 26
- 230000023556 desulfurization Effects 0.000 claims abstract description 26
- 239000001257 hydrogen Substances 0.000 claims abstract description 25
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 25
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000001035 drying Methods 0.000 claims abstract description 20
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 8
- 239000011593 sulfur Substances 0.000 claims abstract description 8
- 239000003463 adsorbent Substances 0.000 claims description 23
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 claims description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- 239000002808 molecular sieve Substances 0.000 claims description 13
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 239000002131 composite material Substances 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 238000012805 post-processing Methods 0.000 claims description 10
- 238000004140 cleaning Methods 0.000 claims description 9
- 230000015572 biosynthetic process Effects 0.000 claims description 7
- 238000003786 synthesis reaction Methods 0.000 claims description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- 239000003034 coal gas Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000004215 Carbon black (E152) Substances 0.000 claims description 5
- 230000002159 abnormal effect Effects 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 238000011010 flushing procedure Methods 0.000 claims description 5
- 229930195733 hydrocarbon Natural products 0.000 claims description 5
- 150000002430 hydrocarbons Chemical class 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000001514 detection method Methods 0.000 claims description 2
- 238000003860 storage Methods 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 15
- 238000004128 high performance liquid chromatography Methods 0.000 abstract 1
- 230000006872 improvement Effects 0.000 description 8
- 238000009835 boiling Methods 0.000 description 5
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 4
- 239000006096 absorbing agent Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 230000001172 regenerating effect Effects 0.000 description 4
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000010297 mechanical methods and process Methods 0.000 description 2
- 239000000741 silica gel Substances 0.000 description 2
- 229910002027 silica gel Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000001960 triggered effect Effects 0.000 description 1
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention provides a purification system of coke oven gas, which relates to the technical field of gas purification and comprises a desulfurization module, a impurity removal module, a compression module and a post-treatment module, wherein the desulfurization module adopts an HPF (high performance liquid chromatography) process to remove sulfur components in the coke oven gas, the impurity removal module adopts a TSA (thermal swing adsorption) process to remove impurity components in the coke oven gas, and the compression module is used for centrifugally compressing purified gas after impurity removal; the post-treatment module comprises a cold box, a PSA hydrogen purification module and a TSA drying moduleA block; the invention adopts TSA impurity removal treatment, cryogenic separation, PSA hydrogen purification and TSA drying means, utilizes TSA temperature swing adsorption technology to deeply remove impurity components such as tar, benzene, naphthalene and the like in the conventional coke oven gas impurity removal process, and completes H through heat exchange and cryogenic separation in a cold box 2 、CO、CH 4 And N 2 The separation of the gas is realized by combining the gas purification treatment and the mixed gas separation, and the method is economical and efficient.
Description
Technical Field
The invention relates to the technical field of gas purification, in particular to a coke oven gas purification system.
Background
At present, the coke oven gas is more purified and treated, generally is taken as a raw material to be sent to a purifying device after being pressurized, the coke oven gas is entrained with tar, benzene, naphthalene and other impurity components, the internal flow passage of a compressor is narrow, the tar, naphthalene and other impurity components contained in the coke oven gas are easier to bond and deposit in a compressor cylinder, the tar, naphthalene and other impurities in the coke oven gas can cause the flow passage of the compressor to be blocked, the gas pumping amount and the pressure ratio of the compressor are smaller than design values, and a compressor anti-surge protection system is triggered to jump, so that the continuous operation period of the coke oven gas compressor is as short as several months to half a year, the shutdown cleaning frequency is too high, and great economic loss is caused;
meanwhile, the technologies of purifying CO from a mixed gas currently commercialized are a cuprammonium solution method, a COSORB method, a cryogenic separation method, and a pressure swing adsorption method (PSA method), which is a new gas separation technology and widely used, which is a method of condensing CO into a liquid state at a low temperature by using the difference of boiling points of components in a mixed gas to be separated, and has disadvantages in that: the water and CO in the raw material gas must be removed 2 The content of the coke oven gas is less than 1ppm, otherwise, the pipeline is blocked at low temperature, so that how to combine gas purification treatment and mixed gas separation to obtain a more economical and efficient method is a problem to be solved, and therefore, the invention provides a coke oven gas purification system to solve the problems in the prior art.
Disclosure of Invention
Aiming at the problems, the invention provides a coke oven gas purifying system which combines gas purifying treatment and mixed gas separation, and is more economical and efficient.
In order to achieve the purpose of the invention, the invention is realized by the following technical scheme: the purifying system of the coke oven gas comprises a desulfurization module, a impurity removal module, a compression module and a post-treatment module, wherein the desulfurization module adopts an HPF process to remove sulfur components in the coke oven gas, the impurity removal module adopts a TSA temperature swing adsorption process to remove impurity components in the coke oven gas, and the compression module is used for centrifugally compressing purified gas after impurity removal;
the post-treatment module comprises a cold box, a PSA hydrogen purification module and a TSA drying module, wherein the cold box is used for carrying out heat exchange and cryogenic separation on purified gas after centrifugal compression to finish H 2 、CO、CH 4 And N 2 Is separated from the cold box H 2 Delivering to PSA hydrogen purification module for purification and TSA drying module for drying, delivering the CO discharged from the cold box to downstream dimethyl carbonate DMC synthesis section, and discharging the CH of the cold box 4 Is used for LNG production.
The further improvement is that: the desulfurization module is a desulfurization tower and is used for controlling the saturation content of naphthalene in the coal gas to be 0.43-0.54 g/m 3 Tar less than 100mg/m 3 Sulfur content < 10ppm.
The further improvement is that: the impurity removal module comprises an adsorption separation reactor group and a pressure swing adsorber group, wherein the pressure swing adsorber group is used for adapting to a TSA temperature swing adsorption process, impurity components in coke oven gas, including tar, naphthalene, benzene and ammonia, are adsorbed by controlling different adsorption pressures, and the gas subjected to impurity removal by adsorption passes through the pressure swing adsorber group and is output to the adsorption separation reactor group.
The further improvement is that: the pressure swing adsorber group is used for desorbing and desorbing impurity components on the adsorbent by closing the pressure of the adsorption bed, increasing the temperature of the bed layer to 80-99 ℃ and adopting a process of flushing with purifying liquid, so that the adsorbent is regenerated.
Further improvement is thatIn the following steps: the adsorption separation reactor group adopts active carbon and 13X molecular sieve to construct a composite bed adsorber, and cooperates with a three-tower adsorption process to adsorb water and CO in the coal gas 2 And the heavy hydrocarbon is removed, and the purified gas after removal enters a compression module.
The further improvement is that: the composite bed adsorber is connected to an adsorption tower in the three-tower adsorption process, and the adsorbent is regenerated by mixing adsorption tail gas and low-pressure nitrogen in the adsorption tower.
The further improvement is that: the compression module comprises a gas cache tank and a gas compressor, wherein the gas compressor is used for centrifugally compressing the removed purified gas, and the gas cache tank is used for temporarily storing the centrifugally compressed purified gas.
The further improvement is that: the exhaust end of the cold box is provided with a gas purity analyzer which is used for exhausting H 2 、CO、CH 4 And carrying out storage detection and feeding back data to the control center.
The further improvement is that: and the control center is internally provided with manifold software and is used for collecting all parameters in the operation process of the desulfurization module, the impurity removal module, the compression module and the post-processing module and the purity of the exhaust gas at the exhaust end of the cold box, and determining the position of the fault module according to the parameter change of the desulfurization module, the impurity removal module, the compression module and the post-processing module when the purity of the exhaust gas is abnormal.
The beneficial effects of the invention are as follows:
1. the invention adopts the means of TSA impurity removal treatment, cryogenic separation, PSA hydrogen purification and TSA drying, and based on the existing coke oven gas impurity removal technology, utilizes TSA temperature swing adsorption technology to deeply remove the impurity components such as tar, benzene, naphthalene and the like, and completes H by heat exchange and cryogenic separation in a cold box 2 、CO、CH 4 And N 2 Is separated from the cold box H 2 Delivering to PSA hydrogen purification and TSA drying, delivering the CO discharged from the cold box to a downstream dimethyl carbonate DMC synthesis section, and discharging the CH of the cold box 4 The method is used for LNG production, so that the combination of gas purification treatment and mixed gas separation is realized, and the method is more economical and efficient.
2. The invention adopts the composite bed adsorber of the active carbon and the 13X molecular sieve, adopts a three-tower process to effectively remove water, CO2 and heavy hydrocarbon components, and avoids equipment freezing and blocking caused by low liquefying temperature of raw material gas.
3. The pressure of the adsorption bed is reduced, the temperature of the bed layer is increased, and the impurity components of the pressure swing adsorber adsorbent are desorbed and desorbed by adopting a flushing means, so that the adsorbent is regenerated, the adsorption tail gas in the adsorption tower and low-pressure nitrogen are mixed for regenerating the adsorbent of the composite bed layer adsorber, and the pressure swing adsorber is convenient to recycle and use efficiently.
4. According to the invention, all parameters in the operation process of the desulfurization module, the impurity removal module, the compression module and the post-processing module and the purity of the exhaust gas at the exhaust end of the cold box are collected through the main pipe software, when the purity of the exhaust gas is abnormal, the position of the fault module is determined according to the parameter changes of the desulfurization module, the impurity removal module, the compression module and the post-processing module, and the functions are diversified.
Drawings
FIG. 1 is a diagram showing the constitution of the present invention.
Detailed Description
The present invention will be further described in detail with reference to the following examples, which are only for the purpose of illustrating the invention and are not to be construed as limiting the scope of the invention.
Example 1
According to the embodiment shown in fig. 1, a purification system of coke oven gas is provided, which comprises a desulfurization module, a impurity removal module, a compression module and a post-treatment module, wherein the desulfurization module adopts an HPF process to remove sulfur components in the coke oven gas, the impurity removal module adopts a TSA temperature swing adsorption process to remove impurity components in the coke oven gas, and the compression module is used for centrifugally compressing purified gas after impurity removal;
the post-treatment module comprises a cold box, a PSA hydrogen purification module and a TSA drying module, wherein the cold box is used for carrying out heat exchange and cryogenic separation on purified gas after centrifugal compression to finish H 2 、CO、CH 4 And N 2 Is separated from the cold box H 2 To PSA hydrogenThe purification module performs purification and the TSA drying module performs drying, the CO discharged from the cold box is sent to a downstream dimethyl carbonate DMC synthesis working section, and the CH discharged from the cold box 4 Is used for LNG production. On the basis of the traditional coke oven gas impurity removal process, the TSA temperature swing adsorption technology is utilized to deeply remove tar, benzene, naphthalene and other impurity components, H2, CO, CH4 and N2 are separated in a cold box through heat exchange and cryogenic separation, H2 from the cold box is sent to a PSA hydrogen purification and TSA drying process, CO from the cold box is sent to a downstream dimethyl carbonate DMC synthesis section, CH4 from the cold box is used for LNG production, and therefore gas purification treatment and mixed gas separation are combined, and the process is more economical and efficient.
Cryogenic separation refers to the use of the boiling point difference of different gases to cool and liquefy the mixed gas under high pressure, so as to achieve the purpose of separating the mixed gas, and mechanical methods such as throttling expansion or adiabatic expansion are generally adopted to compress and cool the gas, and then the difference of the boiling points of different gases is used to rectify the gas, so that the different gases are separated. Is characterized by high purity of the product gas.
Temperature Swing Adsorption (TSA) is a technique applied to regenerate adsorbents. When the PSA uses pressure swing to release the adsorbed gas, the TSA will adjust the temperature to vent the adsorbed gas. TSA technology is based on the handling capacity of certain materials, such as activated carbon, silica gel and silicate, to adsorb gases at moderate temperatures (40 ℃, 100 ℃) and then release the gases by warming to 120 ℃ (250 ℃). TSA may be used to separate a particular gas from a mixed gas. Typically, TSA is passed through a circulation system wherein vessels containing adsorbent material are cooled to produce a dry or clean product gas by sequentially absorbing the target gas, followed by heating.
PSA hydrogen purification technology is a technology that is widely used in hydrogen production and purification processes. Based on the molecular sieve adsorption principle, the hydrogen purification is realized by utilizing the selective adsorption capacity of different adsorption substances on gas molecules. The method comprises the following steps: the pre-cooled compressed air enters a molecular sieve absorber, and a specific adsorbent such as activated carbon or molecular sieve is arranged in the molecular sieve absorber. After the adsorption is completed, hydrogen, argon and the like in the compressed air are adsorbed by the adsorbent, and the rest of the gas components pass through. Triggering the pressure drop signal, entering another adsorber, desorbing the former adsorber, and regenerating the adsorber by using the desorbed gas. By recycling the adsorber and performing alternating adsorption and desorption operations, high purity hydrogen is continuously produced. Simple operation, compact process flow, low equipment investment and operation cost.
The desulfurization module is a desulfurization tower and is used for controlling the saturation content of naphthalene in the coal gas to be 0.43-0.54 g/m 3 Tar less than 100mg/m 3 Sulfur content < 10ppm.
The impurity removal module comprises an adsorption separation reactor group and a pressure swing adsorber group, wherein the pressure swing adsorber group is used for adapting to a TSA temperature swing adsorption process, impurity components in coke oven gas, including tar, naphthalene, benzene and ammonia, are adsorbed by controlling different adsorption pressures, and the gas subjected to impurity removal by adsorption passes through the pressure swing adsorber group and is output to the adsorption separation reactor group. The pressure swing adsorber group is used for desorbing and desorbing impurity components on the adsorbent by closing the pressure of the adsorption bed, increasing the temperature of the bed layer to 80-99 ℃ and adopting a process of flushing with purifying liquid, so that the adsorbent is regenerated. Is convenient for recycling and high-efficiency use.
The adsorption separation reactor group adopts active carbon and 13X molecular sieve to construct a composite bed adsorber, and cooperates with a three-tower adsorption process to adsorb water and CO in the coal gas 2 And the heavy hydrocarbon is removed, and the purified gas after removal enters a compression module. The composite bed adsorber is connected to an adsorption tower in the three-tower adsorption process, and the adsorbent is regenerated by mixing adsorption tail gas and low-pressure nitrogen in the adsorption tower. Is convenient for recycling and high-efficiency use.
The compression module comprises a gas cache tank and a gas compressor, wherein the gas compressor is used for centrifugally compressing the removed purified gas, and the gas cache tank is used for temporarily storing the centrifugally compressed purified gas.
Example two
According to the embodiment shown in fig. 1, a purification system of coke oven gas is provided, which comprises a desulfurization module, a impurity removal module, a compression module and a post-treatment module, wherein the desulfurization module adopts an HPF process to remove sulfur components in the coke oven gas, the impurity removal module adopts a TSA temperature swing adsorption process to remove impurity components in the coke oven gas, and the compression module is used for centrifugally compressing purified gas after impurity removal;
the post-treatment module comprises a cold box, a PSA hydrogen purification module and a TSA drying module, wherein the cold box is used for carrying out heat exchange and cryogenic separation on purified gas after centrifugal compression, the separation of H2, CO, CH4 and N2 is completed, H2 discharged from the cold box is sent to the PSA hydrogen purification module for purification and the TSA drying module for drying, CO discharged from the cold box is sent to a downstream dimethyl carbonate DMC synthesis section, and CH4 discharged from the cold box is used for LNG production. On the basis of the traditional coke oven gas impurity removal process, the TSA temperature swing adsorption technology is utilized to deeply remove tar, benzene, naphthalene and other impurity components, H2, CO, CH4 and N2 are separated in a cold box through heat exchange and cryogenic separation, H2 from the cold box is sent to a PSA hydrogen purification and TSA drying process, CO from the cold box is sent to a downstream dimethyl carbonate DMC synthesis section, CH4 from the cold box is used for LNG production, and therefore gas purification treatment and mixed gas separation are combined, and the process is more economical and efficient.
Cryogenic separation refers to the use of the boiling point difference of different gases to cool and liquefy the mixed gas under high pressure, so as to achieve the purpose of separating the mixed gas, and mechanical methods such as throttling expansion or adiabatic expansion are generally adopted to compress and cool the gas, and then the difference of the boiling points of different gases is used to rectify the gas, so that the different gases are separated. Is characterized by high purity of the product gas.
Temperature Swing Adsorption (TSA) is a technique applied to regenerate adsorbents. When the PSA uses pressure swing to release the adsorbed gas, the TSA will adjust the temperature to vent the adsorbed gas. TSA technology is based on the handling capacity of certain materials, such as activated carbon, silica gel and silicate, to adsorb gases at moderate temperatures (40 ℃, 100 ℃) and then release the gases by warming to 120 ℃ (250 ℃). TSA may be used to separate a particular gas from a mixed gas. Typically, TSA is passed through a circulation system wherein vessels containing adsorbent material are cooled to produce a dry or clean product gas by sequentially absorbing the target gas, followed by heating.
PSA hydrogen purification technology is a technology that is widely used in hydrogen production and purification processes. Based on the molecular sieve adsorption principle, the hydrogen purification is realized by utilizing the selective adsorption capacity of different adsorption substances on gas molecules. The method comprises the following steps: the pre-cooled compressed air enters a molecular sieve absorber, and a specific adsorbent such as activated carbon or molecular sieve is arranged in the molecular sieve absorber. After the adsorption is completed, hydrogen, argon and the like in the compressed air are adsorbed by the adsorbent, and the rest of the gas components pass through. Triggering the pressure drop signal, entering another adsorber, desorbing the former adsorber, and regenerating the adsorber by using the desorbed gas. By recycling the adsorber and performing alternating adsorption and desorption operations, high purity hydrogen is continuously produced. Simple operation, compact process flow, low equipment investment and operation cost.
The exhaust end of the cold box is provided with a gas purity analyzer, and the gas purity analyzer is used for storing and detecting exhausted H2, CO and CH4 and feeding back data to the control center. And the control center is internally provided with manifold software and is used for collecting all parameters in the operation process of the desulfurization module, the impurity removal module, the compression module and the post-processing module and the purity of the exhaust gas at the exhaust end of the cold box, and determining the position of the fault module according to the parameter change of the desulfurization module, the impurity removal module, the compression module and the post-processing module when the purity of the exhaust gas is abnormal. The maintenance and the overhaul are convenient, and the functions are diversified.
The purification system of the coke oven gas adopts the means of TSA impurity removal treatment, cryogenic separation, PSA hydrogen purification and TSA drying, on the basis of the existing coke oven gas impurity removal technology, the TSA temperature swing adsorption technology is utilized to deeply remove the tar, benzene, naphthalene and other impurity components, and H is completed by heat exchange and cryogenic separation in a cold box 2 、CO、CH 4 And N 2 Is separated from the cold box H 2 Sending to PSA hydrogen purification and TSA drying, sending the CO from the cold box to downstream dimethyl carbonate DMC synthesisSection, CH of cold box 4 The method is used for LNG production, so that the combination of gas purification treatment and mixed gas separation is realized, and the method is more economical and efficient. The invention adopts the composite bed adsorber of the active carbon and the 13X molecular sieve, adopts a three-tower process to effectively remove water, CO2 and heavy hydrocarbon components, and avoids equipment freezing and blocking caused by low liquefying temperature of raw material gas. Meanwhile, the pressure of the adsorption bed is reduced, the temperature of the bed layer is increased, and the impurity components of the pressure swing adsorber adsorbent are desorbed and desorbed by adopting a flushing means, so that the adsorbent is regenerated, the adsorption tail gas in the adsorption tower and low-pressure nitrogen are mixed for regenerating the adsorbent of the composite bed layer adsorber, and the pressure swing adsorber is convenient to recycle and use efficiently. In addition, all parameters in the operation process of the desulfurization module, the impurity removal module, the compression module and the post-processing module and the purity of the exhaust gas at the exhaust end of the cold box are collected through the main pipe software, when the purity of the exhaust gas is abnormal, the position of the fault module is determined according to the parameter changes of the desulfurization module, the impurity removal module, the compression module and the post-processing module, and the functions are diversified.
The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (9)
1. The utility model provides a clean system of coke oven gas, includes desulfurization module, edulcoration module, compression module and aftertreatment module, its characterized in that: the desulfurization module adopts an HPF process to remove sulfur components in the coke oven gas, the impurity removal module adopts a TSA temperature swing adsorption process to remove impurity components in the coke oven gas, and the compression module is used for centrifugally compressing the purified gas after impurity removal;
the post-treatment module comprises a cold box, a PSA hydrogen purification module and a TSA drying moduleThe cold box is used for carrying out heat exchange and cryogenic separation on the purified gas after centrifugal compression to finish H 2 、CO、CH 4 And N 2 Is separated from the cold box H 2 Delivering to PSA hydrogen purification module for purification and TSA drying module for drying, delivering the CO discharged from the cold box to downstream dimethyl carbonate DMC synthesis section, and discharging the CH of the cold box 4 Is used for LNG production.
2. A coke oven gas cleaning system according to claim 1, characterized in that: the desulfurization module is a desulfurization tower and is used for controlling the saturation content of naphthalene in the coal gas to be 0.43-0.54 g/m 3 Tar less than 100mg/m 3 Sulfur content < 10ppm.
3. A coke oven gas cleaning system according to claim 2, characterized in that: the impurity removal module comprises an adsorption separation reactor group and a pressure swing adsorber group, wherein the pressure swing adsorber group is used for adapting to a TSA temperature swing adsorption process, impurity components in coke oven gas, including tar, naphthalene, benzene and ammonia, are adsorbed by controlling different adsorption pressures, and the gas subjected to impurity removal by adsorption passes through the pressure swing adsorber group and is output to the adsorption separation reactor group.
4. A coke oven gas cleaning system according to claim 3, characterized in that: the pressure swing adsorber group is used for desorbing and desorbing impurity components on the adsorbent by closing the pressure of the adsorption bed, increasing the temperature of the bed layer to 80-99 ℃ and adopting a process of flushing with purifying liquid, so that the adsorbent is regenerated.
5. A coke oven gas cleaning system according to claim 4, characterized in that: the adsorption separation reactor group adopts active carbon and 13X molecular sieve to construct a composite bed adsorber, and cooperates with a three-tower adsorption process to adsorb water and CO in the coal gas 2 And the heavy hydrocarbon is removed, and the purified gas after removal enters a compression module.
6. A coke oven gas cleaning system according to claim 5, characterized in that: the composite bed adsorber is connected to an adsorption tower in the three-tower adsorption process, and the adsorbent is regenerated by mixing adsorption tail gas and low-pressure nitrogen in the adsorption tower.
7. A coke oven gas cleaning system according to claim 6, characterized in that: the compression module comprises a gas cache tank and a gas compressor, wherein the gas compressor is used for centrifugally compressing the removed purified gas, and the gas cache tank is used for temporarily storing the centrifugally compressed purified gas.
8. A coke oven gas cleaning system according to any one of claims 1-7, characterized in that: the exhaust end of the cold box is provided with a gas purity analyzer which is used for exhausting H 2 、CO、CH 4 And carrying out storage detection and feeding back data to the control center.
9. A coke oven gas cleaning system according to claim 8, characterized in that: and the control center is internally provided with manifold software and is used for collecting all parameters in the operation process of the desulfurization module, the impurity removal module, the compression module and the post-processing module and the purity of the exhaust gas at the exhaust end of the cold box, and determining the position of the fault module according to the parameter change of the desulfurization module, the impurity removal module, the compression module and the post-processing module when the purity of the exhaust gas is abnormal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202311729054.7A CN117866672A (en) | 2023-12-15 | 2023-12-15 | Coke oven gas purifying system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202311729054.7A CN117866672A (en) | 2023-12-15 | 2023-12-15 | Coke oven gas purifying system |
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| Publication Number | Publication Date |
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| CN117866672A true CN117866672A (en) | 2024-04-12 |
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| CN202311729054.7A Pending CN117866672A (en) | 2023-12-15 | 2023-12-15 | Coke oven gas purifying system |
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- 2023-12-15 CN CN202311729054.7A patent/CN117866672A/en active Pending
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