CN220194445U - Membrane separation device in coal clean utilization process - Google Patents
Membrane separation device in coal clean utilization process Download PDFInfo
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- CN220194445U CN220194445U CN202321734650.XU CN202321734650U CN220194445U CN 220194445 U CN220194445 U CN 220194445U CN 202321734650 U CN202321734650 U CN 202321734650U CN 220194445 U CN220194445 U CN 220194445U
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- 239000012528 membrane Substances 0.000 title claims abstract description 152
- 238000000926 separation method Methods 0.000 title claims abstract description 70
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000003245 coal Substances 0.000 title claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 79
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 239000002737 fuel gas Substances 0.000 claims abstract description 10
- 239000012466 permeate Substances 0.000 claims abstract description 10
- 238000004140 cleaning Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 abstract description 12
- 239000002994 raw material Substances 0.000 abstract description 11
- 239000002912 waste gas Substances 0.000 abstract description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 19
- 239000001257 hydrogen Substances 0.000 description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 16
- 238000010248 power generation Methods 0.000 description 11
- 230000008901 benefit Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- 238000002309 gasification Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000012465 retentate Substances 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000012695 Interfacial polymerization Methods 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- -1 alcohol amine Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The utility model discloses a membrane separation device in a coal clean utilization process, which comprises a primary membrane separator, a gas-liquid separator and a secondary membrane separator; the primary membrane separator and the secondary membrane separator are both used for separating the mixed gas into H-enriched gas 2 Permeation and permeation of H-depleted 2 Intercepting gas; the gas-liquid separator is used for separating liquid CO 2 Separating from the gas; a high-temperature resistant separation membrane is arranged in the primary membrane separator; the raw material gas pipeline is connected with a primary membrane separator, the outlet of the permeation side of the primary membrane separator is connected with a fuel gas pipeline, the outlet of the interception side of the primary membrane separator is connected with a gas-liquid separator through a heat exchanger and a condenser, and the outlet of the gas-liquid separator is connected with a secondary membrane separator through the heat exchangerThe method comprises the steps of carrying out a first treatment on the surface of the The permeate side outlet of the second-stage membrane separator is connected with a raw material gas pipeline through a compressor, and the interception side outlet of the second-stage membrane separator is communicated with a waste gas pipeline. The primary membrane separator is provided with a high temperature resistant membrane, so that the cooling process before the membrane is omitted, the cost is saved, and the CO in the raw materials can be recovered efficiently 2 Effectively captures and recovers.
Description
Technical Field
The utility model relates to the technical field of membrane separation, in particular to a membrane separation device in a coal clean utilization process.
Background
The utilization of coal in China is gradually developed to clean, scale and intensify, and the single fuel property is changed to the direction of fuel and raw materials, and the emphasis is on the two directions of modern coal chemical industry and coal-fired power generation. The integrated gasification combined cycle power generation is a power generation technology combining a clean coal gasification technology and high-efficiency gas-steam combined cycle, and is an important development direction of high-efficiency clean coal-fired power generation.
The technology prepares the coal into the synthesis gas (mainly CO and H 2 、CO 2 、N 2 Etc.) CO generation via water gas shift 2 And H 2 CO is then added 2 After removal, the fuel is combusted for the gas turbine. Conversion of CO in gas 2 The concentration is generally 35-45% (v/v), the pressure is high, the impurity is less, and the cost of capturing and removing before combustion is greatly reduced compared with that after combustion, so that the method is also considered as one of important paths for deep emission reduction of greenhouse gases.
CO for the process 2 Trapping and removal are typically carried out by alcohol amine absorption. Due to CO 2 The content is higher, and the absorption method is not economical enough considering investment cost and energy consumption. The membrane separation technology has the advantages of simple operation, small occupied area and high elasticity, and the membrane technology is a pressure-driven separation process, and the economy is more obvious by utilizing the high pressure of the converted air.
However, based on the performance of the current commercial membrane products, the existing membrane separation device can not realize high-efficiency separation of hydrogen and can capture and recycle CO at the same time 2 Obtaining CO capable of subsequent utilization 2 A product; moreover, since the shift gas is at a high temperature (above 150 ℃), a cooling process is usually required before entering the membrane separation, resulting in a complete processAnd the investment of equipment and the running cost of the device are increased.
Thus, a process is provided which can efficiently recover hydrogen while capturing CO without cooling the feed gas before it enters the membrane separator 2 Is necessary.
Disclosure of Invention
The utility model provides a membrane separation device in the clean utilization process of coal, so as to overcome the problems.
In order to achieve the above object, the technical scheme of the present utility model is as follows:
a membrane separation device in the clean utilization process of coal comprises a primary membrane separator, a gas-liquid separator, a secondary membrane separator, a heat exchanger, a condenser and a compressor;
the primary membrane separator and the secondary membrane separator are both used for separating the mixed gas into H-enriched gas 2 Permeation and permeation of H-depleted 2 Intercepting gas; the gas-liquid separator is used for separating liquid CO 2 Separating from the gas;
a high-temperature resistant first separation membrane is arranged in the primary membrane separator;
the feed gas pipeline is connected with the feed inlet of the primary membrane separator, the first permeate side outlet of the primary membrane separator is connected with the fuel gas pipeline, the first interception side outlet of the primary membrane separator is connected with the feed inlet of the gas-liquid separator sequentially through a first pipeline, a heat exchanger, a second pipeline, a condenser and a third pipeline, and the top outlet of the gas-liquid separator is connected with the feed inlet of the secondary membrane separator through a fourth pipeline, the heat exchanger and a fifth pipeline; the second permeate side outlet of the second-stage membrane separator is connected with the raw material gas pipeline through a sixth pipeline, a compressor and a seventh pipeline, and the second interception side outlet of the second-stage membrane separator is communicated with a waste gas pipeline.
Further, the bottom of the gas-liquid separator is connected with a liquid CO separator for separating out 2 An eighth line for discharge.
Further, a high-temperature-resistant second separation membrane is arranged in the second-stage membrane separator.
Further, the first separation membrane and the second separation membrane are both separation membranes having a use temperature of 120 ℃ or higher.
Further, the first separation membrane and the second separation membrane are both separation membranes with the use temperature of 120-180 ℃.
Further, H of the first separation membrane and the second separation membrane 2 /CO 2 The separation coefficient is not less than 20.
Compared with the existing membrane separation equipment, the utility model has the beneficial effects that:
the membrane separation device in the clean utilization process of coal disclosed by the utility model has the advantages that the primary membrane separator is provided with the high-temperature resistant membrane, a cooling device before the membrane is omitted, the structure of the device is simplified, the production cost is saved, and the device can realize the efficient recovery of hydrogen and simultaneously realize the recovery of CO in raw materials 2 Is effectively captured and recovered.
In addition, through the second grade membrane separator that is provided with high temperature resistant membrane, further improve hydrogen recovery, and before hydrogen can high temperature return to first grade membrane separator for the hydrogen that gets into the fuel gas pipeline that whole device separated keeps high temperature, need not to reheat can guarantee gas power generation efficiency.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions of the prior art, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it will be obvious that the drawings in the following description are some embodiments of the present utility model, and that other drawings can be obtained according to these drawings without inventive effort to a person skilled in the art.
Fig. 1 is a schematic diagram of a membrane separation device in a coal cleaning and utilizing process, which is disclosed in an embodiment of the utility model.
In the figure: 1. a primary membrane separator; 101. a first permeate side outlet; 102. a first retentate side outlet; 2. a gas-liquid separator; 201. a top outlet; 3. a second stage membrane separator; 301. a second permeate side outlet; 302. a second retentate side outlet; 4. a heat exchanger; 5. a condenser; 6. a compressor; a. a feed gas line; b. a fuel gas line; c. a first pipeline; d. a second pipeline; e. a third pipeline; f. a fourth pipeline; g. a fifth line; h. a sixth pipeline; i. a seventh pipeline; j. a waste gas line; k. and an eighth pipeline.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present utility model more apparent, the technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments of the present utility model. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
The membrane separation device in the coal clean utilization process provided in the embodiment shown in fig. 1 comprises a primary membrane separator 1, a gas-liquid separator 2, a secondary membrane separator 3, a heat exchanger 4, a condenser 5 and a compressor 6;
the primary membrane separator 1 and the secondary membrane separator 3 are both used for separating the mixed gas into H-enriched gas 2 Permeation and permeation of H-depleted 2 Intercepting gas; the gas-liquid separator 2 is used for separating liquid CO 2 Separating from the gas;
a first high-temperature-resistant separation membrane is arranged in the primary membrane separator 1, the high temperature is not lower than 120 ℃, and the high temperature resistance is not lower than 120 ℃ when the separator is normally used;
the feed gas pipeline a is connected with a feed inlet of the primary membrane separator 1, a first permeation side outlet 101 of the primary membrane separator 1 is connected with a fuel gas pipeline b, a first interception side outlet 102 of the primary membrane separator 1 is sequentially connected with a feed inlet of the gas-liquid separator 2 through a first pipeline c, a heat exchanger 4, a second pipeline d, a condenser 5 and a third pipeline e, and a top outlet 201 of the gas-liquid separator 2 is connected with a feed inlet of the secondary membrane separator 3 through a fourth pipeline f, the heat exchanger 4 and a fifth pipeline g; the second osmosis side of the second-stage membrane separator 3 is dischargedThe port 301 is connected to the raw gas line a through a sixth line h, a compressor 6 and a seventh line i, and the second interception side outlet 302 of the second-stage membrane separator 3 is communicated with an exhaust gas line j; high temperature lean H on the rejection side of the first membrane separator 1 2 The trapped gas enters a heat exchanger 4 for heat exchange to be cooled for the first time, then enters a condenser 5 for secondary cooling, and CO in the trapped gas is removed 2 Condensed and combined with H in the gas-liquid separator 2 2 、CO、N 2 Separating the non-condensable gas, and introducing the non-condensable gas into a heat exchanger 4 to be subjected to high-temperature lean H on the interception side of the first membrane separator 1 2 The trapped gas exchanges heat and heats up, so that heat waste is avoided, energy is saved, and production cost is reduced; high temperature lean H on the interception side of the first membrane separator 1 by the heat exchanger 4 2 The trapped gas is cooled before entering the condenser 5, and the load of the condenser 5 is reduced; the H-enriched separated by the second-stage membrane separator 3 2 The permeation gas enters the compressor 6 through the sixth pipeline H, and enters the raw gas pipeline a to be combined with the raw gas after being pressurized, and the compressor 6 can be rich in H 2 The seepage and ventilation transportation provides power, so that the circulation and separation are facilitated.
The membrane separation device in the clean coal utilization process disclosed by the utility model has the advantages that the primary membrane separator is provided with the high-temperature resistant membrane, a cooling device before the membrane is omitted, the cooling process before raw material gas enters the separation membrane is reduced, the structure of the device is simplified, the production cost is saved, and the device can realize the reduction of CO in raw materials 2 Is effectively trapped and recovered to obtain CO 2 The product can be used subsequently, so that the economic benefit is further improved; the primary membrane separator can separate most of hydrogen in the raw material gas, and the secondary membrane separator can further recycle CO 2 The hydrogen in the liquefied non-condensable gas can be recovered by the arrangement of the primary membrane separator and the secondary membrane separator, and meanwhile, the temperature of the hydrogen separated by the device is high, and the hydrogen can be directly used as fuel gas for energy supply without heating, so that the power generation efficiency of the fuel gas can be ensured.
In a specific embodiment, the bottom of the gas-liquid separator 2 is connected with a liquid CO separator for separating 2 An eighth discharged line k for separating liquid CO from the gas-liquid separator 2 2 Is discharged through an eighth pipeline k, is convenient for liquid CO 2 And (5) recycling and subsequent utilization.
In a specific embodiment, a high temperature resistant second separation membrane is arranged in the secondary membrane separator 3, the high temperature is not lower than 120 ℃, and the high temperature resistant temperature is not lower than 120 ℃ when the separator is normally used, so that the separated H-rich gas is separated 2 The permeation air can keep higher temperature and return to the primary membrane separator 1, so that the hydrogen separated by the device can ensure the efficiency of gas power generation without heating.
In a specific embodiment, the first separation membrane and the second separation membrane are both separation membranes with the use temperature of more than 120 ℃, so that materials enter the first separation membrane without cooling by cooling equipment, and finally separated fuel hydrogen can be ensured without heating, and the gas power generation efficiency is ensured.
In a specific embodiment, the first separation membrane and the second separation membrane are both separation membranes with the use temperature of 120-180 ℃, in this embodiment, the first separation membrane built in the primary membrane separator 1 and the second separation membrane built in the secondary membrane separator 3 are both prepared by adopting the preparation method of the interfacial polymerization membrane disclosed by CN111167320, and the separation membranes are high-temperature resistant and high-H 2 /CO 2 The selective membrane can directly enter the membrane separator for separation without cooling before entering the membrane separator, so that the economic cost is greatly saved, and the separated high-temperature hydrogen is directly conveyed to the gas turbine through the fuel pipeline without heating due to high temperature of the gas entering the membrane separator, thereby ensuring the gas power generation efficiency.
In a specific embodiment, H of the first separation membrane and the second separation membrane 2 /CO 2 A separation coefficient of 20 for ensuring H 2 With CO 2 The separation effect of the gas is improved, so that the hydrogen concentration of the gas is improved, and the gas power generation efficiency is improved; at the same time can reduce CO 2 The low-temperature liquefaction load reduces the equipment investment and the operation energy consumption of the whole device.
The utility model discloses a process flow of a membrane separation device in a coal clean utilization process, which comprises the following steps:
the raw gas is mixed gas (called shift gas) obtained by converting coal gasification synthetic gas by water gas, and the gas quantity is 200000m 3 /hr (177775 Kg/hr), pressure 50barG, temperature 150 ℃, its composition is as follows:
| component (A) | H 2 | CO 2 | CO | N 2 |
| Composition (vol%) | 56.10 | 40.60 | 2.60 | 0.70 |
Because the first separation membrane arranged in the primary membrane separator 1 has high temperature resistance, the raw material gas can directly enter the primary membrane separator 1 through the raw material gas pipeline a without a cooling process; in the primary membrane separator 1, hydrogen preferentially permeates through the first separation membrane and is enriched on the permeation side of the primary membrane separator 1, and the obtained H-enriched gas is enriched 2 Permeate gas is delivered from the first permeate side outlet 101 via fuel gas line b to the gas turbine; lean H obtained on the rejection side of the primary membrane separator 1 2 The trapped gas enters the heat exchanger 4 from the first trapped side outlet 102 through the first pipeline c for heat exchange, and the cooled lean H is generated 2 The trapped gas enters the condenser 5 through the second pipeline d, and the condenser 5 is depleted of H 2 Cooling the trapped gas to-50deg.CCO is caused to be 2 Liquefying, and separating the gas-liquid mixture into liquid CO in the gas-liquid separator 2 via the third pipeline e 2 Is separated and discharged from an eighth pipeline k at the bottom of the gas-liquid separator 2, low-temperature noncondensable gas enters the heat exchanger 4 from a top outlet 201 of the gas-liquid separator 2 through a fourth pipeline f, and is separated from the first-stage membrane separator 1 to obtain high-temperature lean H 2 The trapped gas is subjected to heat exchange, so that the low-temperature non-condensable gas is heated to about 150 ℃ and then enters a secondary membrane separator 3; in the secondary membrane separator 3, hydrogen preferentially permeates through the second separation membrane and is enriched on the permeation side of the secondary membrane separator 3, then enters the compressor 6 through the sixth pipeline h to be pressurized, and then enters the raw gas pipeline a to be combined with raw gas, and hydrogen is further recovered, and the hydrogen contains N 2 And a small amount of CO 2 The trapped gas is discharged from the second trapped side outlet 302 of the second-stage membrane separator 3 through the exhaust gas pipeline j;
wherein the H-enriched gas is fed to the gas turbine via a fuel gas line b 2 The permeation and ventilation volume is 14649Kg/hr, the temperature is 150 ℃, and the composition is as follows:
| component (A) | H 2 | CO 2 | CO | N 2 |
| Composition (vol%) | 97.77 | 2.22 | 0.01 | 0.00 |
Through a two-stage membrane separation process, H 2 The recovery rate reaches 96.93 percent. And H is 2 The concentration is 97.77 percent, the temperature is 150 ℃, and the gas power generation efficiency can be ensured without adding a heating device;
liquid CO discharged through eighth line k 2 Stream, flow 144192Kg/hr, CO 2 Concentration of 97.36%, CO 2 Capturing and removing rate 90.27% to obtain liquid CO 2 Can be used in the fields of agricultural food processing, agricultural production and the like, thereby improving economic benefit.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present utility model, and not for limiting the same; although the utility model 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 scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the utility model.
Claims (6)
1. The membrane separation device in the coal clean utilization process is characterized by comprising a primary membrane separator (1), a gas-liquid separator (2), a secondary membrane separator (3), a heat exchanger (4), a condenser (5) and a compressor (6);
the primary membrane separator (1) and the secondary membrane separator (3) are both used for separating the mixed gas into H-rich gas 2 Permeation and permeation of H-depleted 2 Intercepting gas; the gas-liquid separator (2) is used for separating liquid CO 2 Separating from the gas;
a high-temperature resistant first separation membrane is arranged in the primary membrane separator (1);
the feed gas pipeline (a) is connected with a feed inlet of the primary membrane separator (1), a first permeation side outlet (101) of the primary membrane separator (1) is connected with a fuel gas pipeline (b), a first interception side outlet (102) of the primary membrane separator (1) is sequentially connected with the feed inlet of the gas-liquid separator (2) through a first pipeline (c), a heat exchanger (4), a second pipeline (d), a condenser (5) and a third pipeline (e), and a top outlet (201) of the gas-liquid separator (2) is connected with the feed inlet of the secondary membrane separator (3) through a fourth pipeline (f), the heat exchanger (4) and a fifth pipeline (g); the second permeate side outlet (301) of the second-stage membrane separator (3) is connected with the raw gas pipeline (a) through a sixth pipeline (h), a compressor (6) and a seventh pipeline (i), and the second interception side outlet (302) of the second-stage membrane separator (3) is communicated with an exhaust gas pipeline (j).
2. The membrane separation device in the coal clean utilization process according to claim 1, wherein the bottom of the gas-liquid separator (2) is connected with a liquid CO separator 2 An eighth line (k) being discharged.
3. The membrane separation device in the coal clean utilization process according to claim 1, wherein a high-temperature-resistant second separation membrane is arranged in the secondary membrane separator (3).
4. The membrane separation device in a coal cleaning and utilization process according to claim 3, wherein the first separation membrane and the second separation membrane are both separation membranes with a use temperature of 120 ℃ or higher.
5. The membrane separation device in the coal cleaning and utilizing process according to claim 4, wherein the first separation membrane and the second separation membrane are both separation membranes with the use temperature of 120-180 ℃.
6. A membrane separation device in a coal cleaning and utilization process according to claim 3, wherein the first separation membrane and the second separation membrane are H 2 /CO 2 The separation coefficient is not less than 20.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321734650.XU CN220194445U (en) | 2023-07-04 | 2023-07-04 | Membrane separation device in coal clean utilization process |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202321734650.XU CN220194445U (en) | 2023-07-04 | 2023-07-04 | Membrane separation device in coal clean utilization process |
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| Publication Number | Publication Date |
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| CN220194445U true CN220194445U (en) | 2023-12-19 |
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