CN113769541A - CO generated by washing low-temperature methanol2Preparation of high pressure CO from product gas2Method and apparatus for supporting gas - Google Patents
CO generated by washing low-temperature methanol2Preparation of high pressure CO from product gas2Method and apparatus for supporting gas Download PDFInfo
- Publication number
- CN113769541A CN113769541A CN202111133659.0A CN202111133659A CN113769541A CN 113769541 A CN113769541 A CN 113769541A CN 202111133659 A CN202111133659 A CN 202111133659A CN 113769541 A CN113769541 A CN 113769541A
- Authority
- CN
- China
- Prior art keywords
- gas
- methanol
- water
- temperature
- pressure
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 238000005406 washing Methods 0.000 title claims abstract description 40
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 188
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 80
- 239000007789 gas Substances 0.000 claims abstract description 75
- 238000000034 method Methods 0.000 claims abstract description 28
- 239000012159 carrier gas Substances 0.000 claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 claims abstract description 5
- 238000007906 compression Methods 0.000 claims description 18
- 230000006835 compression Effects 0.000 claims description 16
- 239000003507 refrigerant Substances 0.000 claims description 15
- 230000015572 biosynthetic process Effects 0.000 claims description 11
- 238000003786 synthesis reaction Methods 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 9
- 239000000498 cooling water Substances 0.000 claims description 8
- 239000002826 coolant Substances 0.000 claims description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 5
- 239000012267 brine Substances 0.000 claims description 5
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 claims description 5
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 3
- 239000003245 coal Substances 0.000 abstract description 20
- 238000002309 gasification Methods 0.000 abstract description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 description 41
- 239000000047 product Substances 0.000 description 25
- 239000007788 liquid Substances 0.000 description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 10
- 239000000843 powder Substances 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 239000002817 coal dust Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000012043 crude product Substances 0.000 description 2
- 238000011143 downstream manufacturing Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 241000208125 Nicotiana Species 0.000 description 1
- 235000002637 Nicotiana tabacum Nutrition 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000003607 modifier Substances 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000002123 temporal effect Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/704—Solvents not covered by groups B01D2257/702 - B01D2257/7027
Abstract
The invention discloses a method and equipment for preparing CO2 product gas generated by low-temperature methanol washing into high-pressure CO2 carrier gas, which comprises the step of mixing the carrier gas with CO2At least one CO providing a first pressure connected in series in the direction of flow2A product gas production apparatus, a first-stage compressor and a first cooler, a water washing tower, second-stage to nth-stage compressors and second-to n-1-th coolers disposed after the respective compressors, and a pressure of not less than 8.0MPa and a methanol content of not more than 50mg/Nm obtained by using the above-mentioned apparatus3CO with water content not higher than 1500ppmV2A method of carrying a gas. Wherein CO at a first pressure is provided2The product gas facility comprises a low-temperature methanol washing facility, and the carrier gas is applied to conveying pulverized coal in coal gasification.
Description
Technical Field
The invention belongs to CO2Gas applications, in particular CO produced by low-temperature methanol scrubbing2Preparation of high pressure CO from product gas2The field of carrier gases.
Background
Carbon dioxide (CO)2) The method is widely applied to the industries of chemical industry, machinery, food, agriculture, tobacco and the like, and has high application value in industry. Currently produce CO2Various processes such as ammonia synthesis, methanol synthesis, oxo synthesis, coal gasification, etc., to obtain CO, which is often low in pressure and complex in impurity content2Further pressurization and purification is required to meet the subsequent process requirements.
For example, in coal gasification processes, the constituents produced are CO and H2And mainly comprises CO2By-products of (a). To separate CO2With synthesis gas, removing H contained therein2S, COS and other impurities are washed by low-temperature methanol conventionally
The method of (1). The method utilizes CO and H2And CO2The physical phenomenon that the solubility of gases in methanol at low temperature (-30 ℃ to-50 ℃) is different is adopted, the synthesis gas is separated from byproducts in a methanol washing tower, and then the CO is further purified by flash evaporation and gas stripping2The output temperature is about 40-60 ℃, the pressure is about 0.2-0.5 MPa, and CO is2CO content greater than 97%2And (5) producing gas. CO thus obtained2The product gas was dry but was entrained with about 300-500mg/Nm due to the methanol scrubbing3The methanol gas of (2).
When the coal gasification unit adopts the pulverized coal gasification technology, a large amount of CO with high pressure grade is needed2The carrier gas is used for continuously using the coal powder lock hopper, the ash lock hopper, the coal powder conveying and various blowing. CO in this case2The carrier gas is generally low pressure CO obtained by a low temperature methanol wash process2Pressurizing the product gas to obtain CO after use2Filtering and discharging. With the increasingly strict environmental protection requirements, the CO discharged finally2The content of methanol in the tail gas is not higher than 50mg/Nm3(GB 31571-2015). Therefore, the CO must be pretreated2The methanol content of the product gas is 500mg/Nm3Down to 50mg/Nm3The following; meanwhile, in order to avoid wet adhesion of the pulverized coal in the conveying process, a carrier gas is requiredThe water content in the product is controlled below 1500 ppmV.
CN107399737B discloses a preparation method of high-pressure gas-phase carbon dioxide for high-pressure pulverized coal gasification, which is characterized in that cold energy generated by a low-temperature methanol washing process is utilized to pre-cool a feed gas, and then cryogenic separation is carried out to prepare medium-pressure liquid CO2The obtained medium-pressure liquid CO2After being pressurized by a low-temperature liquid pump, the medium-pressure liquid CO is recovered by the low-temperature methanol washing process2The cold energy of (2) is gasified to generate high-pressure gas-phase CO2And sent to the upstream pulverized coal gasification unit. This patent does not disclose how to saturate the CO present in the gaseous state2The methanol content in the product gas is reduced to 50mg/Nm3The following is a description.
In view of the above, how to design a new process flow to eliminate the above-mentioned defects and shortcomings of the prior art and obtain high pressure CO with very low methanol content and water content2Gas is a subject to be solved by those skilled in the art.
Disclosure of Invention
How to design an economic, efficient and simple method for introducing CO with lower pressure (less than or equal to 0.5MPa)2The product gas is prepared into high-pressure (more than or equal to 8.0MPa) CO with methanol and water content meeting the requirement2The carrier gas is a technical problem to be solved by the invention.
In order to solve the technical problem, the invention discloses a method for preparing CO2Means for supporting the gas, the means comprising means for supporting the gas along the CO2At least one CO providing a first pressure connected in series in the direction of flow2Plant for producing a gas, a first compressor and a first cooler, a water scrubber, a second to an nth compressor and a second to an n-1 cooler arranged after the respective compressors, wherein the compressed CO is compressed by n stages2The pressure of carrier gas is not less than 8.0MPa, and CO is2The content of methanol in the carrier gas is not higher than 50mg/Nm3The water content is not higher than 1500 ppmV.
In one aspect, the invention provides CO at a first pressure2The product gas equipment is low-temperature methanol washing equipment for treating the synthesis gas, and the first pressure is not higher than 0.5 MPa.
In one aspect, the cooling medium in the first cooler is cooling water having a temperature of not higher than 35 ℃, and the cooling medium in the second to n-1 th coolers is an organic refrigerant or a frozen brine having a temperature of not higher than 15 ℃, the organic refrigerant containing liquid ammonia or propylene and being prepared by an ice maker.
In another aspect, the water wash column of the present invention is connected to the methanol-water separation column of the low temperature methanol wash unit by a conduit.
It is a further object of the present invention to disclose a process for the preparation of CO using the apparatus as described above2A method of carrying a gas, wherein,
a) providing CO at a first pressure2The product gas is the mixture of the gas and the water,
b) introducing CO2The product gas is pressurized and cooled in a first stage compressor and a first cooler,
c) CO compressed by the first stage compressor2Washing methanol in a water washing tower to obtain CO after methanol removal2，
d) Removing the methanol of CO2Pressurizing to not less than 8.0MPa in the second to nth compressors, condensing in the second to n-1 coolers arranged after the corresponding compressors to remove the water contained therein, and obtaining CO2The content of methanol in the carrier gas is not higher than 50mg/Nm3The water content is not higher than 1500 ppmV.
Further, the methanol removed from the water washing tower is transported to a methanol-water separation tower in a low-temperature methanol washing unit, and the methanol is recovered by rectification.
Further, CO treated by the n-1 th cooler2The temperature of the product gas is not higher than 25 ℃.
Compared with the prior art, the technical scheme provided by the invention has the following advantages:
washing with water to remove CO2The methanol in the product is recovered by rectification in a methanol-water separation tower, and the mature process can efficiently and simply reduce the content of the methanol.
By multi-stage compression of CO2Product gas, the relative positions between the washing tower and the stages of compression being arranged strategically, e.g. washing the waterThe tower is arranged after the first-stage compression, so that the volume of gas entering the water washing tower is reduced, the corresponding tower diameter can be reduced on the premise of not obviously increasing the equipment investment, and the manufacturing cost and the occupied area of the water washing tower are reduced.
Different cooling media are used in the first cooler and the second to n-1 th coolers. The former can use common cooling water with the temperature of 30-40 ℃, and the common cooling water is easy to obtain and has low cost; a cooling medium having a lower temperature (not higher than 15 ℃) such as an organic refrigerant or frozen brine is used in the second to n-1 coolers to saturate the water with CO after washing2The water in the gas is removed by means of condensation. The low-temperature methanol washing device is matched with an auxiliary organic refrigeration ice machine unit, so that additional devices are not needed for obtaining the low-temperature cooling medium.
No cooler is arranged after the nth stage compressor, and CO is kept2The carrier gas enters the next working procedure at a higher temperature (80-100 ℃), so that the energy consumption and the equipment cost are saved.
Drawings
The advantages and spirit of the present invention can be further understood by the following detailed description of the invention and the accompanying drawings.
FIG. 1 is a schematic flow chart depicting a comparative example of the present invention;
FIG. 2 is a schematic flow diagram of one embodiment of the present invention.
Detailed Description
Specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings. However, it is to be understood that the present invention is not limited to such an embodiment described below, and the technical idea of the present invention may be implemented in combination with other known techniques or other techniques functionally equivalent to those known techniques.
In the following description of specific embodiments, the present invention will be described with reference to numerous directional terms in order to clearly illustrate the process and apparatus of the present invention, but the terms "upper", "lower", "front", "rear", "outer", "inner", "outward", "inward", and the like should be construed as words of convenience and not as words of limitation.
Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not intended to limit the temporal order, quantity, or importance, but are not intended to indicate or imply relative importance or implicitly indicate the number of technical features indicated, but merely to distinguish one technical feature from another technical feature in the present disclosure. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically stated otherwise. Similarly, the appearances of the phrases "a" or "an" in various places herein are not necessarily all referring to the same quantity, but rather to the same quantity, and are intended to cover all technical features not previously described. Similarly, unless a specific number of a claim recitation is intended to cover both the singular and the plural, and embodiments may include a single feature or a plurality of features. Similarly, modifiers similar to "about", "approximately" or "approximately" that occur before a numerical term herein typically include the same number, and their specific meaning should be read in conjunction with the context.
Unless clearly indicated to the contrary, each aspect or embodiment defined herein may be combined with any other aspect or embodiments. In particular, any feature indicated as being preferred or advantageous may be combined with any other feature indicated as being preferred or advantageous.
In the present invention, syngas means that the main components are CO and H2A process gas mixture according to (1) can be prepared by coal gasification. The prepared crude product also contains CO2、H2S, etc. by-products by low temperature methanol washing (e.g. using
) Separating the crude product to obtain purified CO and H2And CO in an amount greater than 97%, even 98.5%2Product gas, this CO2The product gas contains 300-500 mg-Nm3The methanol of (1). ppmV is the unit of volume content, ppm is 10-6Thus, a water content of 1500ppmV refers to the volume content of water vapor in the gas, i.e. the molar content is 0.0015. mg/Nm3Refers to the number of milligrams contained in a standard cubic meter volume.
CO2The pressure of the product gas is in the range of 0.2-0.5 MPa, and downstream processes, such as CO conveying coal dust2The pressure range of the carrier gas is required to be higher than 8.0MPa (depending on the type of coal gasification). The carrier gas is to be understood in a broad sense here to include CO2The gas does not participate in chemical reactions under various conditions, and can be pulverized coal conveying gas and purge gas in the pulverized coal gasification technology, inert protective gas required in other process flows, carbon dioxide supplement and utilization and the like. CO in the present invention2The product gas is always compressed in the gaseous state, which is generally 2-3 for the compression of the gas compressor, based on CO2The initial pressure of the gas and the desired final pressure can be calculated to yield the desired number of compression stages. In order to protect the compressor, improve the compression efficiency, and reduce the compression energy consumption, it is conventional to provide a gas-liquid separator at its inlet, followed by an interstage cooler. The interstage cooler selects a heat exchanger which is not in direct contact with the gas, and uses cooling water or other refrigerants to exchange heat with the compressed gas so as to reduce the temperature of the gas. Compressed CO2The temperature of the gas is generally higher than 70 ℃ and possibly higher than 80 ℃, and the temperature of the cooling water at the temperature of 30-40 ℃ can be reduced to about 40 ℃; and the refrigerant or frozen brine with the temperature of about 5-10 ℃ can be cooled to about 20 ℃. CO22The lower the temperature of the gas, the lower its saturated water content, and the greater the amount of condensed water produced during cooling. The refrigerant is conventionally selected from organic refrigerants such as liquid ammonia or propylene, and also from frozen brine, to obtain the desired temperature of the refrigerant in the ice machine. The lower the temperature of the refrigerant is, the greater the energy consumption of the ice maker is, so that the temperature of the refrigerant is reasonably determined according to the temperature required by the cooled gas to achieve the purpose of reducing the energy consumption.
In the present invention, gaseous CO2Methanol (MeOH) vapor contained in (c) was removed in a water washing column. CO22Enters from the bottom of the water washing tower and rises, washing water is sprayed down from the top of the water washing tower, when the washing water and the washing water are contacted, MeOH is dissolved in water and taken away, and purified CO2And discharged from the top. The water washing step may be to remove CO2The content of methanol in the methanol is reduced to not more than 50mg/Nm3But will raise the water content above 10000 ppmV. This portion of water exceeding the carrier gas requirement is removed by condensation in the various interstage coolers by the methods mentioned above. The water dissolved with the methanol is conveyed into a methanol and water separation tower, and enters a downstream process after rectification and separation. The size of the water scrubber is determined by the volume of the gas to be treated, and the smaller the volume of the gas, the smaller the diameter of the water scrubber.
Fig. 1 shows a comparative example of the present invention. The raw synthesis gas 1 fed to the low-temperature methanol washing device a is separated in the device a into a purified synthesis gas 2 and CO2Product gas 3, the latter flow being 40000Nm3H, pressure of 0.26MPa, temperature of 35 deg.C, water content of zero, methanol content of 500mg/Nm3。CO2The product gas 3 enters from the bottom of the water scrubber E, the desalted water 6 is sprayed from the top of the water scrubber, and the two streams are in contact with each other, namely CO2The MeOH in the product gas 3 is carried away by the desalted water 6, while its water content increases. Thus, the demethanized CO withdrawn from the top of the water scrubber E2Methanol content of stream 8 was reduced to less than 50mg/Nm3While the water content increased to 13000 ppmV. The MeOH entrained desalted water 7 enters the methanol-water separation column for further processing for downstream discharge or recovery. CO after demethanol2Stream 8 then undergoes 5 stages of compression, each stage comprising a gas-liquid separator B1-B5 located before compressor C1-C5, and an interstage cooler D1-D5 located after compressor C1-C5, each interstage cooler being cooled with cooling water at a temperature of 33 ℃, with condensed water produced in each gas-liquid separator and each interstage cooler being fed to the process condensate system. For example, in the first stage of compression, the CO after demethanization2Stream 8 after passing through gas-liquid separator B1 gives CO2Stream 4, at constant pressure, slightly elevated to 40 ℃ and a water content of about-13000 ppmV. Through a first stage compressor C1 andCO obtained after the first cooler D12Stream 5 was at a pressure of 0.96MPa, a temperature of 40 ℃ and a water content of still-13000 ppmV, at which temperature and pressure no condensate was present. However, CO2Stream 5 is compressed in second to fifth stages to obtain CO2Stream 9, at a pressure of 5.53MPa, temperature of 40 ℃ and water content of-3400 ppmV. Due to the required CO2The pressure of the carrier gas is above 8MPa, and a sixth stage of compression is arranged, comprising a sixth stage gas-liquid separator B6 and a sixth stage of compressor C6, but no aftercooler is included. This is because the coal powder requires a high temperature carrier gas for transportation, and the energy is wasted by cooling and then heating the coal powder. However, for certain CO requiring ambient or cold streams2An aftercooler may be added for carrier gas applications. CO obtained after six-stage compression2Carrier gas 10 at a pressure of 8.1MPa, a temperature of 40 ℃, a water content of 3400ppmV and methanol of less than 50mg/Nm3. The methanol content of the coal dust meets the requirement, but the water content is too high, so that the wet viscosity of the coal dust can be caused when the coal dust is conveyed. In addition, 40000Nm for handling a pressure of 0.26MPa3CO of/h2The inner diameter of the product gas washing tower is 1900 mm.
Fig. 2 shows an embodiment of the invention. The raw synthesis gas 1 fed to the low-temperature methanol washing device a is separated in the device a into a purified synthesis gas 2 and CO2Product gas 3, the latter flow being 40000Nm3H, pressure of 0.26MPa, temperature of 35 deg.C, water content of zero, methanol content of 500mg/Nm3. Unlike the comparative example in FIG. 1, the present invention is first directed to CO2The product gas 3 undergoes a first stage of compression. CO22The product gas 3 is processed by a gas-liquid separator B1 to obtain CO2Stream 4, which is at constant pressure and temperature, has approximately zero water content. After passing through a first stage compressor C1 and a first cooler D1 with cooling water at a temperature of 33 ℃ to obtain CO2The pressure of the stream 5 is 0.50MPa, the temperature is 40 ℃, the water content is still zero, the volume of the stream 5 is reduced by about half relative to the volume of the stream 3 due to compression, the inner diameter of a required water washing tower is reduced from 1900mm to 1600mm, the manufacturing cost is reduced, and the occupied area is saved. The first cooler D1 can also be usedThe cooler refrigerant achieves the cooling effect, but is not required.
CO compressed in one stage2Stream 5 enters from the bottom of the water scrubber E, desalted water 6 is sprayed from the top of the water scrubber, and the two streams are in contact with CO2The MeOH in stream 5 is carried away by the desalted water 6, while its water content increases. Thus, the demethanized CO withdrawn from the top of the water scrubber E2Methanol content of stream 8 was reduced to less than 50mg/Nm3While the water content increased to 10000 ppmV. The MeOH entrained desalted water 7 enters the methanol and water separation column for further processing for downstream discharge or recovery. CO after demethanol2Stream 8 then undergoes 4 stages of compression, each stage of compression comprising a gas-liquid separator B2-B5 located before compressor C2-C5, and intercoolers D2-D5 located after compressor C2-C5, each intercoolers being cooled with a refrigerant at 0 ℃. For example, propylene is used as the refrigerant. The condensed water produced in each gas-liquid separator and each interstage cooler is fed to a process condensate system. CO after demethanol2Stream 8 is compressed in second to fifth stages to obtain CO2Stream 9, pressure 5.53MPa, temperature 20 ℃ and water content 1300 ppmV. Due to the required CO2The carrier gas pressure is above 8MPa, and a sixth stage compression is provided, including a sixth stage gas-liquid separator B6 and a sixth stage compressor C6, but not including an aftercooler. This is because the coal powder requires a high temperature carrier gas for transportation, and the energy is wasted by cooling and then heating the coal powder. However, for certain CO requiring ambient or cold streams2An aftercooler may be added for carrier gas applications. CO obtained after six-stage compression2Carrier gas 10 at a pressure of 8.1MPa, temperature of 78.2 deg.C, water content of 1300ppmV, methanol content of less than 50mg/Nm3. Not only the methanol content meets the requirement of environmental protection, but also the water content ensures the efficiency of pulverized coal transportation.
The embodiments described in the specification are only preferred embodiments of the present invention, and the above embodiments are only used to illustrate the technical solutions of the present invention and not to limit the present invention. Those skilled in the art can obtain technical solutions through logical analysis, reasoning or limited experiments according to the concepts of the present invention, and all such technical solutions are within the scope of the present invention.
Claims (9)
1. CO generated by washing low-temperature methanol2Preparation of high pressure CO from product gas2Means for supporting the gas, characterised by containing the gas along the CO2The flow direction is connected in sequence:
a) at least one CO providing a first pressure2The equipment for producing the gas comprises a gas production device,
b) a first stage compressor and a first cooler,
c) the water is used for washing the tower,
d) second to nth stage compressors and second to n-1 th coolers disposed after the respective compressors,
wherein, after n-stage compression, CO is obtained2The pressure of carrier gas is not less than 8.0MPa, and CO is2The content of methanol in the carrier gas is not higher than 50mg/Nm3The water content is not higher than 1500 ppmV.
2. The apparatus of claim 1, wherein the first pressure is not greater than 0.5 MPa.
3. The apparatus of claim 1, wherein the CO at the first pressure is provided2The product gas equipment is low-temperature methanol washing equipment for treating synthesis gas.
4. The apparatus of claim 1, wherein the cooling medium in the first cooler is cooling water having a temperature of not higher than 35 ℃.
5. The apparatus according to claim 4, wherein the cooling medium in the second to n-1 th coolers is an organic refrigerant or a frozen brine having a temperature of not higher than 15 ℃.
6. The apparatus of claim 5, wherein the organic refrigerant comprises liquid ammonia or propylene and is produced by an ice-making machine.
7. The apparatus of claim 3, wherein the water washing column is connected to a methanol-water separation column of the low temperature methanol washing apparatus via a pipe to recover and treat methanol from the washing water.
8. Production of CO using the apparatus according to claim 12A method of supporting a gas, characterized in that,
a) providing CO at a first pressure2The product gas is the mixture of the gas and the water,
b) introducing CO2The product gas is pressurized and cooled in a first stage compressor and a first cooler,
c) CO compressed by the first stage compressor2Washing methanol in a water washing tower to obtain CO after methanol removal2，
d) Removing the methanol of CO2Pressurizing to not less than 8.0MPa in the second to nth compressors, condensing in the second to n-1 coolers arranged after the corresponding compressors to remove the water contained therein, and obtaining CO2The content of methanol in the carrier gas is not higher than 50mg/Nm3The water content is not higher than 1500 ppmV.
9. The method of claim 8, wherein the CO after the treatment in the n-1 st cooler2The temperature of the product gas is not higher than 20 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111133659.0A CN113769541A (en) | 2021-09-26 | 2021-09-26 | CO generated by washing low-temperature methanol2Preparation of high pressure CO from product gas2Method and apparatus for supporting gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111133659.0A CN113769541A (en) | 2021-09-26 | 2021-09-26 | CO generated by washing low-temperature methanol2Preparation of high pressure CO from product gas2Method and apparatus for supporting gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113769541A true CN113769541A (en) | 2021-12-10 |
Family
ID=78853680
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111133659.0A Withdrawn CN113769541A (en) | 2021-09-26 | 2021-09-26 | CO generated by washing low-temperature methanol2Preparation of high pressure CO from product gas2Method and apparatus for supporting gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113769541A (en) |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101666573A (en) * | 2009-09-21 | 2010-03-10 | 华北电力大学 | CO2 separation and compression integrated method |
| CN102517086A (en) * | 2011-11-28 | 2012-06-27 | 河南龙宇煤化工有限公司 | Method for using carbon dioxide as delivery gas and back flushing gas of coal powder instead of nitrogen in coal gasification methanol preparation process |
| US20120260801A1 (en) * | 2011-04-14 | 2012-10-18 | Mitsubishi Heavy Industries, Ltd. | Co2 recovery system and recovery method for moisture containing co2 gas |
| US20130078115A1 (en) * | 2010-06-11 | 2013-03-28 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for drying and compressing a co2-rich stream |
| CN103717292A (en) * | 2011-07-25 | 2014-04-09 | 乔治洛德方法研究和开发液化空气有限公司 | Process and apparatus for cooling and compressing a wet gas rich in carbon dioxide |
| CN105120984A (en) * | 2013-04-30 | 2015-12-02 | 株式会社Ihi | Alkalinity control agent supply method and apparatus for compressor impurity separation mechanism |
| CN107311173A (en) * | 2017-08-09 | 2017-11-03 | 惠生工程（中国）有限公司 | A kind of preparation method of high pressure vapor carbon dioxide for coal gasification unit |
| CN210340344U (en) * | 2019-06-14 | 2020-04-17 | 中石化宁波工程有限公司 | Device for removing methanol in carbon dioxide by water washing method |
| CN111747411A (en) * | 2020-07-15 | 2020-10-09 | 广州市华达石化有限公司 | Low-pressure low-temperature treatment method for industrial carbon dioxide gas |
| CN213294699U (en) * | 2020-09-11 | 2021-05-28 | 中国天辰工程有限公司 | Removing CO from coal transportation2Novel system for neutralizing methanol |
-
2021
- 2021-09-26 CN CN202111133659.0A patent/CN113769541A/en not_active Withdrawn
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101666573A (en) * | 2009-09-21 | 2010-03-10 | 华北电力大学 | CO2 separation and compression integrated method |
| US20130078115A1 (en) * | 2010-06-11 | 2013-03-28 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for drying and compressing a co2-rich stream |
| US20120260801A1 (en) * | 2011-04-14 | 2012-10-18 | Mitsubishi Heavy Industries, Ltd. | Co2 recovery system and recovery method for moisture containing co2 gas |
| CN103717292A (en) * | 2011-07-25 | 2014-04-09 | 乔治洛德方法研究和开发液化空气有限公司 | Process and apparatus for cooling and compressing a wet gas rich in carbon dioxide |
| CN102517086A (en) * | 2011-11-28 | 2012-06-27 | 河南龙宇煤化工有限公司 | Method for using carbon dioxide as delivery gas and back flushing gas of coal powder instead of nitrogen in coal gasification methanol preparation process |
| CN105120984A (en) * | 2013-04-30 | 2015-12-02 | 株式会社Ihi | Alkalinity control agent supply method and apparatus for compressor impurity separation mechanism |
| CN107311173A (en) * | 2017-08-09 | 2017-11-03 | 惠生工程（中国）有限公司 | A kind of preparation method of high pressure vapor carbon dioxide for coal gasification unit |
| CN210340344U (en) * | 2019-06-14 | 2020-04-17 | 中石化宁波工程有限公司 | Device for removing methanol in carbon dioxide by water washing method |
| CN111747411A (en) * | 2020-07-15 | 2020-10-09 | 广州市华达石化有限公司 | Low-pressure low-temperature treatment method for industrial carbon dioxide gas |
| CN213294699U (en) * | 2020-09-11 | 2021-05-28 | 中国天辰工程有限公司 | Removing CO from coal transportation2Novel system for neutralizing methanol |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108458549B (en) | System and method for extracting helium from natural gas and liquefying same | |
| CN103523751B (en) | Device and method for performing cryogenic separation and purification on carbon monoxide and hydrogen | |
| CN105865147A (en) | System and method for preparing high purity carbon monoxide and hydrogen-enriched co-production liquid methane | |
| CN107399737B (en) | Preparation method of high-pressure gas-phase carbon dioxide for high-pressure pulverized coal gasification | |
| CN106440661B (en) | Energy-saving device and method for preparing high-purity liquid carbon dioxide | |
| CN1952569A (en) | Process and equipment for liquefying air-containing coal-bed gas | |
| CN101590364A (en) | Gas and synthetic ammonia purge and basin gas are carried out method and the device that hydrogen reclaims | |
| CN114518016A (en) | Carbon dioxide capturing, liquefying and recycling device and method | |
| CN112229143A (en) | Device and method for producing oxygen and nitrogen by separating air through cryogenic rectification | |
| CN107311173B (en) | Preparation method of high-pressure gas-phase carbon dioxide for pulverized coal gasification unit | |
| CN113769541A (en) | CO generated by washing low-temperature methanol2Preparation of high pressure CO from product gas2Method and apparatus for supporting gas | |
| CN106979665B (en) | Method and equipment for purifying synthetic gas | |
| CN103361138B (en) | Method for preparing liquefied natural gas and synthesis ammonia raw material gases by use of hydrogen extraction desorption gas | |
| CN203474449U (en) | Device for separating and purifying carbon monoxide and hydrogen in cryogenic separation mode | |
| CN102706101B (en) | Air separating device | |
| CN214371298U (en) | Carbon dioxide gathering liquefaction recovery device | |
| CN213578367U (en) | Device for producing oxygen and nitrogen by separating air through cryogenic rectification | |
| CN101493277B (en) | Low temperature separation method and apparatus for mine gas | |
| CN113566493A (en) | Cryogenic separation system for helium recovery | |
| CN215886383U (en) | Integrated unit for processing crude synthesis gas and producing carbon dioxide liquid product | |
| CN114165987A (en) | Liquid carbon dioxide production device and production method thereof | |
| CN207831794U (en) | A kind of adipic acid tail gas purifies the device of liquid laughing gas processed | |
| CN202470621U (en) | Air separation system | |
| CN111365941A (en) | Compression liquefaction device based on carbon dioxide entrapment | |
| CN111004081A (en) | Separation method and device for preparing ethylene reaction gas through oxidative coupling of methane |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WW01 | Invention patent application withdrawn after publication |
Application publication date: 20211210 |
|
| WW01 | Invention patent application withdrawn after publication |