CN217526935U - Hydrogen desicator moisture trace impurity is regenerating unit after saturation - Google Patents
Hydrogen desicator moisture trace impurity is regenerating unit after saturation Download PDFInfo
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- CN217526935U CN217526935U CN202220554018.6U CN202220554018U CN217526935U CN 217526935 U CN217526935 U CN 217526935U CN 202220554018 U CN202220554018 U CN 202220554018U CN 217526935 U CN217526935 U CN 217526935U
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Abstract
The utility model discloses a regenerating unit after hydrogen dryer moisture trace impurity saturation relates to methyl alcohol hydrogen manufacturing equipment technical field, solves the unable regeneration or the difficult technical problem of regeneration after current hydrogen dryer moisture and trace impurity absorption saturation, including installing regeneration pipeline, regeneration blow-down pipeline and the nitrogen gas input tube on methyl alcohol hydrogen manufacturing device, the one end of regeneration pipeline communicates with methyl alcohol hydrogen manufacturing device's hydrogen dryer exit end, and the other end communicates before the water cooler shell side of methyl alcohol hydrogen manufacturing device, and the one end of regeneration blow-down pipeline communicates with methyl alcohol hydrogen manufacturing device's hydrogen dryer entry end, and the other end communicates with methyl alcohol hydrogen manufacturing device's blow-down device, be provided with first valve and temperature measurement point on the regeneration pipeline, be provided with the second valve on the regeneration blow-down pipeline, the nitrogen gas input tube communicates with methyl alcohol hydrogen manufacturing's heat exchanger, is provided with the nitrogen gas valve on this nitrogen gas input tube; the utility model discloses realize quick regeneration, practice thrift investment cost.
Description
Technical Field
The utility model relates to a methyl alcohol hydrogen manufacturing equipment technical field, more specifically relate to a regenerating unit technical field after hydrogen dryer moisture trace impurity saturation.
Background
With the continuous progress of science and technology and the high-speed development of industries such as integrated circuits, hydrogen has wide application in industry; in recent years, due to the rapid development of hydrogen peroxide prepared by fine chemical engineering and anthraquinone method, powder metallurgy, grease hydrogenation, hydrogenation of forestry products and agricultural products, bioengineering, hydrogenation of petroleum refining, clean automobiles using hydrogen fuel and the like, the demand for pure hydrogen is rapidly increased; for areas without convenient hydrogen sources, if the traditional method for separating and producing hydrogen by using petroleum, natural gas or coal as raw materials is adopted, huge investment is needed, hydrogen can be conveniently produced by electrolyzing water by medium and small users, but the energy consumption is large, the hydrogen consumption per cubic meter reaches about 6 ℃, the hydrogen purity is not ideal, impurities are more, and the scale is also limited, so that in recent years, a plurality of original hydrogen production manufacturers using electrolyzed water are subjected to technical transformation, a new process route for converting methanol and water vapor into hydrogen is adopted, the methanol vapor hydrogen production method is a hydrogen production technology developed abroad in the 20 th century 80 th, the investment is low, the construction is quick, no emission and pollution are caused, and the raw material availability is high; the hydrogen production process at home and abroad is mature, the highly integrated technology and the fuel cell power generation technology are successfully applied to the fields of new energy automobiles, communication stations and the like, and the application prospect is very good.
During the trial operation of the methanol hydrogen production device, the quality of the product hydrogen is reduced along with the time, wherein the water content in the high-purity hydrogen is higher, and can reach 60ppm (the index is less than or equal to 3 ppm) at the highest, so that the product quality of a company is seriously influenced; the process judges that the adsorption capacity of the drying agent is deteriorated, so that water molecules in the product hydrogen overflow and the aim of dry adsorption cannot be fulfilled; however, when the hydrogen dryer is operated for a long time, the hydrogen dryer cannot be regenerated or is difficult to regenerate after moisture and trace impurities are adsorbed and saturated, if the hydrogen dryer is completely and thoroughly regenerated, the process requirements are met, firstly, the adsorbent in the dryer needs to be replaced, secondly, regeneration equipment needs to be invested and installed, the investment cost is high in technical improvement of the existing process, and the energy consumption is high in the regeneration process.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a: in order to solve unable regeneration or regeneration difficulty behind hydrogen desicator moisture and the trace impurity absorption saturation when methyl alcohol hydrogen plant technology is long-time moving, frequent problem is changed to dry adsorbent, the utility model provides a regenerating unit behind hydrogen desicator moisture trace impurity saturation, to the drier by conduction oil heat transfer heating nitrogen gas, reach regeneration and use, solve product purity problem in time fast.
The utility model adopts the technical scheme as follows: a regeneration device of a hydrogen dryer after being saturated with trace impurities comprises a regeneration pipeline, a regeneration vent pipeline and a nitrogen input pipe which are arranged on a methanol hydrogen production device, wherein one end of the regeneration pipeline is communicated with the outlet end of the hydrogen dryer of the methanol hydrogen production device, the other end of the regeneration pipeline is communicated with the front of a water cooler shell pass inlet valve of the methanol hydrogen production device, one end of the regeneration vent pipeline is communicated with the inlet end of the hydrogen dryer of the methanol hydrogen production device, the other end of the regeneration vent pipeline is communicated with the vent device of the methanol hydrogen production device, a first valve and a temperature measuring point are arranged on the regeneration pipeline, a second valve is arranged on the regeneration vent pipeline, the nitrogen input pipe is communicated with a heat exchanger of the methanol hydrogen production device, and a nitrogen valve is arranged on the nitrogen input pipe; the nitrogen exchanges heat through the shell pass of the vaporization superheater and the high-temperature heat conduction oil passing through the shell pass of the reactor, the heat is recovered through the heat exchanger, the nitrogen enters the hydrogen dryer through the regeneration pipeline and is continuously discharged to complete the complete regeneration of the hydrogen dryer, and the temperature measuring point on the regeneration pipeline is not lower than 220 ℃ in the regeneration process.
The methanol hydrogen production device comprises a vaporization superheater, a reactor, a heat exchanger, a water cooler, a washing tower, a gas-liquid separator, a mixed gas buffer tank, an adsorption tower, a hydrogen buffer tank, a hydrogen dryer, a hydrogen compressor, an emptying device, a desalted water tank, a hydrogen finished product output pipe, a nitrogen input pipe, a raw material mixing liquid input pipe, a heat-conducting oil inlet and a heat-conducting oil outlet, wherein the vaporization superheater is communicated with the reactor, the vaporization superheater is communicated with the heat-conducting oil inlet, and the reactor is communicated with the heat-conducting oil outlet; the shell side of the heat exchanger is respectively communicated with the tube side of the vaporization superheater, the tube side of the reactor, the shell side of the water cooler, the nitrogen input tube and the raw material mixing liquid input tube, one end of the washing tower is communicated with the water cooler, the other end of the washing tower is sequentially communicated with the gas-liquid separator, the mixed gas cache tank, the adsorption tower, the hydrogen cache tank, the hydrogen dryer and the hydrogen compressor, the outlet of the hydrogen compressor is communicated with the hydrogen finished product output tube, a valve is arranged on the hydrogen finished product output tube, the washing tower and the gas-liquid separator are further communicated with the desalted water tank, and the mixed gas cache tank is further communicated with the emptying device.
The raw material mixing liquid input pipe is provided with a feeding valve, so that feeding is conveniently controlled.
And a water cooler shell pass inlet valve is arranged on a pipeline for communicating the heat exchanger with the water cooler, and is used for closing the communication between the water cooler and the heat exchanger when the hydrogen dryer needs to be regenerated.
The adsorption tower comprises a first adsorption tower and a second adsorption tower, the outlet end of the mixed gas buffer tank is divided into three branches, one branch is communicated with an emptying device, the other two branches are respectively communicated with the first adsorption tower and the second adsorption tower, the inlet and the outlet of the first adsorption tower and the outlet of the second adsorption tower are respectively provided with a valve, the inlet end of the emptying device is provided with an emptying valve, a main valve is arranged on the outlet end main pipe of the mixed gas buffer tank, the first adsorption tower and the second adsorption tower can be used independently, and the main valve, the valve and the emptying valve are arranged to facilitate the on-off control of the main valve, the valve and the emptying valve, so that the adsorption and the desorption are alternately circulated, and the hydrogen with higher purity enters the hydrogen buffer tank.
And valves are respectively arranged on pipelines of the desalted water tank, which are respectively communicated with the washing tower and the gas-liquid separator, so that the control is convenient.
The output of hydrogen buffer tank is provided with hydrogen buffer tank back valve, conveniently closes the intercommunication of hydrogen desicator and hydrogen buffer tank.
The input of hydrogen compressor is provided with the hydrogen compressor inlet valve, conveniently closes the intercommunication of hydrogen desicator and hydrogen compressor.
To sum up, owing to adopted above-mentioned technical scheme, the beneficial effects of the utility model are that:
the utility model discloses can accomplish regeneration after hydrogen dryer moisture content and impurity adsorption saturation when long-time operation, utilize the temperature of conduction oil and nitrogen gas heat transfer can satisfy regenerated requirement completely, need not often change the adsorbent, also need not increase professional regeneration facility, realize quick regeneration, practice thrift investment cost.
Drawings
The invention will now be described, by way of example, with reference to the accompanying drawings, in which:
FIG. 1 is a schematic flow chart of the present invention;
labeled as: 1-vaporization superheater, 2-reactor, 3-heat exchanger, 4-water cooler, 5-washing tower, 6-gas-liquid separator, 7-mixed gas buffer tank, 8-first adsorption tower, 9-second adsorption tower, 10-hydrogen buffer tank, 11-hydrogen drier, 12-hydrogen compressor, 13-emptying device, 14-desalted water tank, 15-hydrogen finished product output pipe, 16-nitrogen input pipe, 17-raw material blending liquid input pipe, 18-heat transfer oil inlet, 19-heat transfer oil outlet, 20-temperature measuring point, 21-regeneration pipeline, 22-regeneration emptying pipeline, A1-first valve, A2-second valve, B1-hydrogen buffer tank rear valve, B2-hydrogen compressor inlet valve, C1-feed valve, C2-water cooler shell side inlet valve, C3-nitrogen valve and C4-emptying valve.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of the embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the present invention, presented in the accompanying drawings, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
Example 1
As shown in fig. 1, the present embodiment provides a regeneration device after saturation of trace impurities in moisture in a hydrogen dryer, which includes a regeneration pipeline 21, a regeneration vent pipeline 22 and a nitrogen input pipe 16, which are installed on a methanol hydrogen production device, wherein one end of the regeneration pipeline 21 is communicated with an outlet end of a hydrogen dryer 11 of the methanol hydrogen production device, the other end of the regeneration pipeline 21 is communicated with a front of a water cooler shell-side inlet valve C2 of the methanol hydrogen production device, one end of the regeneration vent pipeline 22 is communicated with an inlet end of the hydrogen dryer 11 of the methanol hydrogen production device, the other end of the regeneration vent pipeline 22 is communicated with a vent device 13 of the methanol hydrogen production device, a first valve A1 and a temperature measurement point 20 are arranged on the regeneration pipeline 21, a second valve A2 is arranged on the regeneration vent pipeline 22, the nitrogen input pipe 16 is communicated with a heat exchanger 3 of the methanol hydrogen production device, and a nitrogen valve C3 is arranged on the nitrogen input pipe 16; the nitrogen exchanges heat through the shell pass of the vaporization superheater 1 and the high-temperature heat conducting oil through the shell pass of the reactor 2, the heat is recovered through the heat exchanger 3, the nitrogen enters the hydrogen dryer 11 through the regeneration pipeline 21 and is continuously discharged to complete the complete regeneration of the hydrogen dryer 11, and the temperature measuring point 20 on the regeneration pipeline 21 is not lower than 220 ℃ in the regeneration process.
Example 2
On the basis of the embodiment 1, the methanol hydrogen production device comprises a vaporization superheater 1, a reactor 2, a heat exchanger 3, a water cooler 4, a washing tower 5, a gas-liquid separator 6, a mixed gas buffer tank 7, an adsorption tower, a hydrogen buffer tank 10, a hydrogen dryer 11, a hydrogen compressor 12, a blowdown device 13, a desalted water tank 14, a hydrogen finished product output pipe 15, a nitrogen input pipe 16, a raw material mixed liquid input pipe 17, a heat conduction oil inlet 18 and a heat conduction oil outlet 19, wherein the vaporization superheater 1 is communicated with the reactor 2, the vaporization superheater 1 is communicated with the heat conduction oil inlet 18, and the reactor 2 is communicated with the heat conduction oil outlet 19; the shell pass of the heat exchanger 3 is respectively communicated with the tube pass of the vaporization superheater 1, the tube pass of the reactor 2, the shell pass of the water cooler 4, the nitrogen input tube 16 and the raw material mixing liquid input tube 17, one end of the washing tower 5 is communicated with the water cooler 4, the other end of the washing tower 5 is sequentially communicated with the gas-liquid separator 6, the mixed gas buffer tank 7, the adsorption tower, the hydrogen buffer tank 10, the hydrogen dryer 11 and the hydrogen compressor 12, the outlet of the hydrogen compressor 12 is communicated with the hydrogen finished product output tube 15, a valve is arranged on the hydrogen finished product output tube 15, wherein the washing tower 5 and the gas-liquid separator 6 are also communicated with the desalted water tank 14, and the mixed gas buffer tank 7 is also communicated with the emptying device 13.
Example 3
On the basis of the embodiment 2, the raw material mixing liquid input pipe 17 is provided with a feed valve C1, so that feeding is conveniently controlled.
Example 4
On the basis of the embodiment 2, a water cooler 4 shell-side inlet valve is arranged on a pipeline for communicating the heat exchanger 3 with the water cooler 4, and is used for closing the communication between the water cooler 4 and the heat exchanger 3 when the hydrogen dryer 11 needs to be regenerated.
Example 5
On the basis of embodiment 2, the adsorption tower includes a first adsorption tower 8 and a second adsorption tower 9, the outlet end of the mixed gas buffer tank 7 is divided into three branches, one branch is communicated with an emptying device 13, the other two branches are respectively communicated with the first adsorption tower 8 and the second adsorption tower 9, the inlet and the outlet of the first adsorption tower 8 and the outlet of the second adsorption tower 9 are respectively provided with a valve, the inlet end of the emptying device 13 is provided with an emptying valve C4, the outlet end main pipe of the mixed gas buffer tank 7 is provided with a main valve, the first adsorption tower 8 and the second adsorption tower 9 can be used independently, and the main valve, the valve and the emptying valve C4 are arranged to facilitate the alternate circulation of adsorption and desorption through the on-off control of the main valve, the valve and the emptying valve C4, so that the hydrogen with high purity enters the hydrogen buffer tank.
Example 6
On the basis of embodiment 2, the pipeline of the desalted water tank 14, which is respectively communicated with the washing tower 5 and the gas-liquid separator 6, is respectively provided with a valve, so that the control is convenient.
Example 7
On the basis of embodiment 2, the output end of the hydrogen buffer tank 10 is provided with a hydrogen buffer tank rear valve B1, which facilitates closing the communication between the hydrogen dryer 11 and the hydrogen buffer tank 10.
Example 8
On the basis of embodiment 2, the input end of the hydrogen compressor 12 is provided with a hydrogen compressor inlet valve B2, which facilitates closing the communication between the hydrogen dryer 11 and the hydrogen compressor 12.
The utility model discloses a theory of operation does: the utility model discloses if after the desicator adsorption efficiency descends, lead to hydrogen purity to reach the requirement, when the device need park regeneration hydrogen desicator 11, stop the feeding to the device, guarantee that heat conduction oil system normal operating sets for the temperature of advancing vaporization over heater 1 entry on heat conduction oil PLC operating panel at 240 ℃, close feed valve C1 simultaneously, open nitrogen gas valve C3 and let in heat exchanger 3 tube side with nitrogen gas, then pass through the tube side of vaporization over heater 1, the tube side of reactor 2, the shell side of heat exchanger 3, behind the shell side of water cooler 4. After passing through the washing tower 5, the gas-liquid separator 6 and the mixed gas buffer tank, the mixed gas in the reaction system is completely replaced through the vent valve C4, the vent valve C4 is closed, the back valve B1 of the hydrogen buffer tank is closed, the inlet valve B2 of the hydrogen compressor is closed, the inlet valve C2 of the shell pass of the water cooler is closed, the first valve A1 on the newly-added regeneration pipeline 21 and the second valve A2 on the regeneration vent pipeline 22 are opened at the same time, heat exchange is carried out on nitrogen entering the system and high-temperature heat conduction oil passing through the shell pass of the vaporization superheater 1 and the shell pass of the reactor 2 at the moment, heat is recycled through the heat exchanger 3, the nitrogen enters the hydrogen dryer 11 through the regeneration pipeline 21 and then is continuously vented to complete the complete regeneration of the hydrogen dryer 11, and the temperature measuring point 20 on the regeneration pipeline 21 is not lower than 220 ℃ in the regeneration process.
The existing methanol hydrogen production process comprises the steps of firstly mixing methanol and desalted water in proportion (mass ratio is 1; the converted mixed gas enters a mixed gas buffer tank, and enters a PSA hydrogen extraction device to adsorb CO in the mixed gas through an adsorbent under the conditions of normal temperature and high pressure 2 CO and other impurity components are not easy to adsorb hydrogen, and when the mixed gas passes through the bed layer of the purification tower, CO is adsorbed 2 CO and other impurities overflow hydrogen, when the adsorbent absorbs a certain amount of impurities, the hydrogen is reversely discharged, and CO is discharged under the condition of low pressure 2 CO and the like are desorbed from the adsorbent, so that the adsorbent is regenerated; through the alternate circulation of adsorption and desorption, the obtained hydrogen with high purity enters a hydrogen buffer tank, then enters a hydrogen dryer 11 to continuously remove trace moisture and impurities in the hydrogen, but if the adsorption capacity of a drying agent is poor under the condition of long-time operation of the device, water molecules in the product hydrogen overflow, and the purpose of dry adsorption cannot be achieved, the adsorbent in the regeneration dryer is considered, a DN50 regeneration pipeline 21 is arranged before the mixed gas enters a water cooler shell side inlet valve C2 in the prior process flow, the front position of an inlet valve B2 of a hydrogen compressor is arranged, a first valve A1 and a temperature measuring point 20 are arranged on the regeneration pipeline 21, a regeneration vent pipeline 22 is arranged at the inlet of the hydrogen dryer 11 and the rear position of a rear valve B1 of the hydrogen buffer tank, the regeneration vent pipeline 22 is connected to a vent device 13, a second valve A2 is arranged on the regeneration vent pipeline 22, and the hydrogen dryer 11 is vented reverselyThe discharged water and trace impurities are discharged into the emptying device 13 for processing, and the regeneration of the hydrogen drier 11 is completed.
Claims (8)
1. The regeneration device comprises a regeneration pipeline (21), a regeneration vent pipeline (22) and a nitrogen input pipe (16), wherein the regeneration pipeline (21), the regeneration vent pipeline (22) and the nitrogen input pipe (16) are installed on a methanol hydrogen production device, one end of the regeneration pipeline (21) is communicated with the outlet end of a hydrogen dryer (11) of the methanol hydrogen production device, the other end of the regeneration pipeline (21) is communicated with the front of a water cooler shell pass inlet valve C2 of the methanol hydrogen production device, one end of the regeneration vent pipeline (22) is communicated with the inlet end of the hydrogen dryer (11) of the methanol hydrogen production device, the other end of the regeneration vent pipeline (22) is communicated with a vent device (13) of the methanol hydrogen production device, a first valve A1 and a temperature measuring point (20) are arranged on the regeneration pipeline (21), a second valve A2 is arranged on the regeneration vent pipeline (22), the nitrogen input pipe (16) is communicated with a heat exchanger (3) of the methanol hydrogen production device, and a nitrogen valve C3 is arranged on the nitrogen input pipe (16).
2. The hydrogen dryer moisture trace impurity saturation regenerating device according to claim 1, wherein the methanol hydrogen production device comprises a vaporization superheater (1), a reactor (2), a heat exchanger (3), a water cooler (4), a washing tower (5), a gas-liquid separator (6), a mixed gas buffer tank (7), an adsorption tower, a hydrogen buffer tank (10), a hydrogen dryer (11), a hydrogen compressor (12), an emptying device (13), a desalted water tank (14), a hydrogen finished product output pipe (15), a nitrogen input pipe (16), a raw material mixed liquid input pipe (17), a heat conduction oil inlet (18) and a heat conduction oil outlet (19), wherein the vaporization superheater (1) is communicated with the reactor (2), the vaporization superheater (1) is communicated with the heat conduction oil inlet (18), and the reactor (2) is communicated with the heat conduction oil outlet (19); the shell side of the heat exchanger (3) is respectively communicated with the tube side of the vaporization superheater (1), the tube side of the reactor (2), the shell side of the water cooler (4), the nitrogen input tube (16) and the raw material mixing liquid input tube (17), one end of the washing tower (5) is communicated with the water cooler (4), the other end of the washing tower (5) is sequentially communicated with the gas-liquid separator (6), the mixed gas buffer tank (7), the adsorption tower, the hydrogen buffer tank (10), the hydrogen dryer (11) and the hydrogen compressor (12), the outlet of the hydrogen compressor (12) is communicated with a hydrogen finished product output tube (15), a valve is arranged on the hydrogen finished product output tube (15), wherein the washing tower (5) and the gas-liquid separator (6) are further communicated with the desalted water tank (14), and the mixed gas buffer tank (7) is further communicated with the emptying device (13).
3. The regeneration device of claim 2, wherein the raw material mixing liquid input pipe (17) is provided with a feed valve C1.
4. The hydrogen dryer moisture trace impurity saturation regenerating device according to claim 2, characterized in that a water cooler shell side inlet valve C2 is arranged on a pipeline of the heat exchanger (3) and the water cooler (4).
5. The device for regenerating a hydrogen dryer after being saturated with trace impurities in water content according to claim 2, wherein the adsorption tower comprises a first adsorption tower (8) and a second adsorption tower (9), the outlet end of the mixed gas buffer tank (7) is divided into three branches, one branch is communicated with the emptying device (13), the other two branches are respectively communicated with the first adsorption tower (8) and the second adsorption tower (9), the inlet and the outlet of the first adsorption tower (8) and the second adsorption tower (9) are respectively provided with a valve, the inlet end of the emptying device (13) is provided with an emptying valve C4, and the main pipe of the outlet end of the mixed gas buffer tank (7) is provided with a master valve.
6. The regeneration device of claim 2, wherein the desalted water tank (14) is provided with valves on the pipelines respectively communicated with the washing tower (5) and the gas-liquid separator (6).
7. The regeneration device of the hydrogen drier after being saturated with trace impurities and water according to claim 2, characterized in that the output end of the hydrogen buffer tank (10) is provided with a hydrogen buffer tank back valve B1.
8. A hydrogen drier regeneration device after saturation of trace impurities in water according to claim 2, characterized in that the input of the hydrogen compressor (12) is provided with a hydrogen compressor inlet valve B2.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220554018.6U CN217526935U (en) | 2022-03-14 | 2022-03-14 | Hydrogen desicator moisture trace impurity is regenerating unit after saturation |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220554018.6U CN217526935U (en) | 2022-03-14 | 2022-03-14 | Hydrogen desicator moisture trace impurity is regenerating unit after saturation |
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| CN217526935U true CN217526935U (en) | 2022-10-04 |
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