CN208561684U - Hydrogen making by natural gas reformation periodic off-gases recyclable device - Google Patents
Hydrogen making by natural gas reformation periodic off-gases recyclable device Download PDFInfo
- Publication number
- CN208561684U CN208561684U CN201820857450.6U CN201820857450U CN208561684U CN 208561684 U CN208561684 U CN 208561684U CN 201820857450 U CN201820857450 U CN 201820857450U CN 208561684 U CN208561684 U CN 208561684U
- Authority
- CN
- China
- Prior art keywords
- periodic
- entrance
- outlet
- gas
- heat exchanger
- 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.)
- Active
Links
Landscapes
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a kind of hydrogen making by natural gas reformation periodic off-gases recyclable devices, belong to chemical emission recycling field.Described device includes: absorption tower, and the unstripped gas entrance on absorption tower is connected with the first periodic off-gases output channel；First end entrance of First Heat Exchanger, First Heat Exchanger is connected with absorb the bottom of the tower outlet；The first end of desorber unit, desorber unit is connected with the outlet of the first end of First Heat Exchanger, and the second end of desorber unit is connected with the second end entrance of First Heat Exchanger, and the second end outlet of First Heat Exchanger is connected with the top entry on absorption tower；Hydrogen recovery unit, hydrogen recovery unit one end is connected with the top exit on absorption tower, the other end is connected with PSA unit.First PSA periodic off-gases generate rich amine solution and periodic off-gases purified gas after the decarburization of absorption tower, and rich amine solution enters desorber unit after First Heat Exchanger exchanges heat and desorbed, and obtain carbon dioxide；Periodic off-gases purified gas, which enters after hydrogen recovery unit reaction, exports hydrogen product through PSA unit.
Description
Technical field
The utility model relates to chemical emission recovery technology field, in particular to a kind of hydrogen making by natural gas reformation periodic off-gases return
Receiving apparatus.
Background technique
Hydrogen is the main raw material of industry and most important industrial gasses and special gas, in petrochemical industry, electronics work
Industry, metallurgical industry, food processing, float glass, Minute Organic Synthesis, aerospace etc. have a wide range of applications.Meanwhile
Hydrogen is also a kind of ideal secondary energy sources.Since the height of hydrogen is fuel, aerospace industry uses liquid hydrogen as fuel.Hydrogen Energy simultaneously
It is generally acknowledged clean energy resource, is showing one's talent as low-carbon and the zero carbon energy.
Gas water steam reforming (Steam Methane Reforming, SMR) is that cost is most in current process for making hydrogen
Low, the maximum method of hydrogen manufacturing amount.The industrial hydrogen of high-purity can be obtained subsequently through pressure-variable adsorption (PSA), but can arrange simultaneously
Amplification quantity PSA periodic off-gases, containing components such as carbon dioxide, hydrogen, carbon monoxide and methane in periodic off-gases, if be directly discharged into big
Gas not only causes energy waste, also will cause atmosphere pollution.Processing method traditional at present is defeated using periodic off-gases as fuel gas
Hydrogen and carbon dioxide content to reburner as fuel, but in PSA periodic off-gases is higher, therefore using PSA periodic off-gases as combustion
Material, the recovery rate for not only reducing hydrogen cause the waste of hydrogen resources, also, since carbon dioxide itself cannot burn also not
The combustion-supporting consumption that also will increase fuel.
Utility model content
The purpose of the utility model is to provide a kind of hydrogen making by natural gas reformation periodic off-gases recyclable devices, to gas renormalizing system
Hydrogen and carbon dioxide in hydrogen PSA periodic off-gases are separated and recovered, and have both improved hydrogen recovery rate, while obtain carbon dioxide
To recycling.
To achieve the above object, the utility model provides a kind of hydrogen making by natural gas reformation periodic off-gases recyclable device, comprising:
Absorption tower, the unstripped gas entrance on the absorption tower are connected with the first periodic off-gases output channel, for the first PSA to speed
Carbon dioxide in deflation, which react with the poor amine liquid in the absorption tower, generates rich amine solution and periodic off-gases purified gas；
First Heat Exchanger, the first end entrance of the First Heat Exchanger are connected with absorb the bottom of the tower outlet, and described the
One heat exchanger using the poor amine liquid in desorber unit with the rich amine solution for being exchanged heat；
The first end of desorber unit, the desorber unit is connected with the outlet of the first end of the First Heat Exchanger, institute
The second end for stating desorber unit is connected with the second end entrance of the First Heat Exchanger, and the second of the First Heat Exchanger brings out
Mouth is connected with the top entry on the absorption tower, and the desorber unit obtains poor amine for desorbing to the rich amine solution
Liquid and carbon dioxide；
Hydrogen recovery unit, described hydrogen recovery unit one end is connected with the top exit on the absorption tower, the other end with
PSA unit is connected, and the hydrogen recovery unit is used to the carbon monoxide in the periodic off-gases purified gas being changed into carbon dioxide,
Become gas in generation, hydrogen product and the 2nd PSA periodic off-gases are exported after the PSA unit pressure-variable adsorption.
Further, the desorber unit includes:
Desorber, the inlet of the desorber are connected with the outlet of the first end of the First Heat Exchanger, the desorber
Outlet at bottom be connected with the second end entrance of the First Heat Exchanger, for the rich amine solution carry out air lift remove titanium dioxide
Carbon；
Reboiler, the reboiler are connected with the bottom of the desorber, for further to the rich amine solution decarburization；
First gas-liquid separator, first gas-liquid separator are connected with the top exit of the desorber, are used for gas-liquid
The carbon dioxide is obtained after isolating free water.
Further, the desorber unit further include:
The entrance of first cooler, first cooler is connected with the top exit of the desorber, and described first is cold
But the outlet of device is connected with the entrance of first gas-liquid separator；
Reflux pump, the entrance of the reflux pump are connected with the liquid-phase outlet of first gas-liquid separator, the reflux pump
Outlet be connected with the reflux water inlet of the desorber.
Further, the hydrogen recovery unit includes:
Compressor, the entrance of the compressor are connected with the top exit on the absorption tower, for compressing the periodic off-gases
Purified gas；
The entrance of second gas-liquid separator, second gas-liquid separator is connected with the outlet of the compressor, is used for gas
Liquid separates the periodic off-gases purified gas；
Second heat exchanger, the gaseous phase outlet phase of the first end entrance of second heat exchanger and second gas-liquid separator
Even, the middle change gas that second heat exchanger is used to generate using shift-converter and the periodic off-gases purified gas after gas-liquid separation
It exchanges heat；
Shift-converter, the entrance of the shift-converter are connected with the outlet of the first end of second heat exchanger, are used for
Carbon monoxide in the periodic off-gases purified gas is changed into carbon dioxide, the outlet of the shift-converter is changed with described second
Second end entrance of hot device is connected, and the second end outlet of the shift-converter is connected with PSA unit.
Further, the hydrogen recovery unit further includes third cooler, the entrance of the third cooler with it is described
The outlet of compressor is connected, and the outlet of the third cooler is connected with the entrance of second gas-liquid separator.
Further, the hydrogen recovery unit further include:
Heater, the entrance of the heater are connected with the outlet of the first end of second heat exchanger, the heater
Outlet is connected with the entrance of the shift-converter；
The entrance of 4th cooler, the 4th cooler is connected with the outlet of the second end of second heat exchanger, described
The outlet of 4th cooler is connected with the entrance of the PSA unit.
Further, described device further include:
The entrance of first circulation pump, the first circulation pump is connected with absorb the bottom of the tower outlet, the first circulation
The outlet of pump is connected with the first end of the First Heat Exchanger；
The entrance of second cooler, second cooler is connected with the outlet of the second end of the First Heat Exchanger, described
The outlet of second cooler is connected with the top entry on the absorption tower.
Further, described device further includes return line, and one end of the return line is connected to the first circulation
On pipeline between the outlet of pump and the first end entrance of the First Heat Exchanger；The other end of the return line is connected to institute
It states on the pipeline between the second end outlet of First Heat Exchanger and the entrance of second cooler.
Further, described device further includes liquid knockout, the entrance of the liquid knockout and the absorption tower top exit phase
Even, the first outlet of the liquid knockout is connected with the liquid return hole on the absorption tower, the second outlet of the liquid knockout and the pressure
The entrance of contracting machine is connected.
The one or more technical solutions provided in the utility model embodiment, at least have the following technical effect that or excellent
Point:
The hydrogen making by natural gas reformation periodic off-gases recyclable device provided in the utility model embodiment, comprising: absorption tower, it is described
The unstripped gas entrance on absorption tower is connected with the first periodic off-gases output channel, for by the first PSA periodic off-gases carbon dioxide with
Poor amine liquid in the absorption tower carries out reaction and generates rich amine solution and periodic off-gases purified gas；First Heat Exchanger, first heat exchange
First end entrance of device is connected with absorb the bottom of the tower outlet, and the First Heat Exchanger is used for using poor in desorber unit
Amine liquid exchanges heat with the rich amine solution；Desorber unit, first end and the First Heat Exchanger of the desorber unit
First end outlet is connected, and the second end of the desorber unit is connected with the second end entrance of the First Heat Exchanger, and described the
The second end outlet of one heat exchanger is connected with the top entry on the absorption tower, and the desorber unit is used for the rich amine solution
It is desorbed, obtains poor amine liquid and carbon dioxide；Hydrogen recovery unit, described hydrogen recovery unit one end and the absorption tower
Top exit is connected, the other end is connected with PSA unit, and the hydrogen recovery unit is used for one in the periodic off-gases purified gas
Carbonoxide is changed into carbon dioxide, becomes gas in generation, and hydrogen product and the 2nd PSA are exported after the PSA unit pressure-variable adsorption
Periodic off-gases.In this way, in hydrogen making by natural gas reformation PSA periodic off-gases hydrogen and carbon dioxide separate and recover, height can be obtained
The carbon dioxide and hydrogen of purity, had both improved hydrogen recovery rate, while recycle carbon dioxide.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of hydrogen making by natural gas reformation periodic off-gases recyclable device provided by the embodiment of the utility model；
Fig. 2 is hydrogen making by natural gas reformation periodic off-gases recovery method flow chart provided by the embodiment of the utility model.
In figure, 1- the first periodic off-gases output channel, the absorption tower 2-, 3- first circulation pump, 4- First Heat Exchanger, 5- reflux
Pipeline, 6- desorber, 7- reboiler, the first cooler of 8-, the first gas-liquid separator of 9-, 10-CO2Output channel, 11- condensed water
Reflux line, 12- reflux pump, 13- second circulation pump, the second cooler of 14-, 15- liquid knockout, 16- compressor, 17- third are cold
But device, the second gas-liquid separator of 18-, 19- drainpipe, the second heat exchanger of 20-, 21- heater, 22- shift-converter, 23-
Four coolers, 24-PSA unit, 25- hydrogen output channel, 26- the second periodic off-gases output channel.
Specific embodiment
This application provides a kind of hydrogen making by natural gas reformation periodic off-gases recyclable device, which not only can be improved existing natural
The hydrogen product rate of gas reforming hydrogen production device, moreover it is possible to which trapping and subsequent recycling are carried out to the carbon dioxide in PSA periodic off-gases
It utilizes, to reduce carbon emission amount, while reducing the consumption of fuel.
The technical solution of the utility model is described further below by drawings and the specific embodiments.
The present embodiment provides a kind of hydrogen making by natural gas reformation periodic off-gases recyclable devices, as shown in Figure 1, described device includes:
Absorption tower 2, First Heat Exchanger 4, desorber unit and hydrogen recovery unit；Wherein,
The unstripped gas entrance on the absorption tower 2 is connected with the first periodic off-gases output channel 1, is used for the first PSA periodic off-gases
In carbon dioxide and the poor amine liquid in the absorption tower 2 react and generate rich amine solution and periodic off-gases purified gas.Wherein, pass through
The first periodic off-gases output channel 1 being connected with the first PSA unit transports to the first PSA periodic off-gases in absorption tower 2, and the first PSA speeds
The poor amine liquid entered at the top of carbon dioxide and absorption tower 2 in deflation generates rich amine solution and periodic off-gases purified gas after being reacted.
Here, described " the first PSA off-gas " is to be discharged in hydrogen making by natural gas reformation technique by the PSA that the first PSA unit discharges
Gas, the main component in periodic off-gases are hydrogen, nitrogen, carbon monoxide, carbon dioxide, methane, argon gas etc..Here, described "
One PSA unit " is the PSA unit in hydrogen making by natural gas reformation technique, not the application hydrogen making by natural gas reformation release gas recovery
In device described " PSA unit 24 ".Amine liquid is used to absorbing carbon dioxide, and the rich amine solution refers to the amine after absorbing carbon dioxide
Liquid；The poor amine liquid refers to the amine liquid after desorbing carbon dioxide；The periodic off-gases purified gas refers to that carbon dioxide is inhaled by amine liquid
Periodic off-gases after receipts.
The first end entrance (rich amine solution entrance) of the First Heat Exchanger 4 passes through pipeline and 2 outlet at bottom of absorption tower
It is connected, the First Heat Exchanger 4 using the poor amine liquid of high temperature in desorber unit with the rich amine solution for being exchanged heat, with right
The rich amine solution heats up；Wherein, the First Heat Exchanger 4 is specially poor rich amine solution heat exchanger.
The first end of the desorber unit is connected with the outlet of the first end of the First Heat Exchanger 4, the desorber list
The second end of member is connected with the second end entrance of the First Heat Exchanger 4, the second end of the First Heat Exchanger 4 export with it is described
The top entry on absorption tower 2 is connected, and the desorber unit obtains poor amine liquid and dioxy for desorbing to the rich amine solution
Change carbon.
Here, referring to Fig. 1, the desorber unit includes:
Desorber 6, (rich amine solution goes out for the first end outlet of the inlet on 6 top of desorber and the First Heat Exchanger 4
Mouthful) be connected, the outlet at bottom of the desorber 6 is connected with the second end entrance (poor amine liquid entrance) of the First Heat Exchanger 4, uses
In to rich amine solution progress air lift carbon dioxide removal；Wherein, rich amine solution from absorption tower 2 with from the poor of desorber 6
After amine liquid exchanges heat in First Heat Exchanger 4, the rich amine solution after heat exchange enters in desorber 6, is desorbed in desorber 6, raw
At poor amine liquid and carbon dioxide.
Reboiler 7, the reboiler 7 are connected with the bottom of the desorber 6, for further de- to the rich amine solution
Carbon；Wherein, by reboiler 7 to the further heat penetration decarburization of rich amine solution, the poor amine liquid of high temperature is flowed by 6 bottom of desorber after decarburization
The poor amine liquid entrance for entering First Heat Exchanger 4, exchanges heat with rich amine solution, heats up to rich amine solution.
First gas-liquid separator 9, first gas-liquid separator 9 are connected with the top exit of the desorber 6, are used for gas
Liquid obtains the carbon dioxide after isolating free water；Wherein, first gas-liquid separator 9 is specially carbon dioxide product gas
Gas-liquid separator carries out gas-liquid separation to the carbon dioxide desorbed in desorber 6, and the carbon dioxide after isolating free water produces
Product pass through CO by gaseous phase outlet2Output channel 10 exports.
Here, in order to cool down to the carbon dioxide desorbed in desorber 6, referring to Fig. 1, the desorber unit is also
Including the first cooler 8, the entrance of first cooler 8 is connected with the top exit of the desorber 6, and described first is cooling
The outlet of device 8 is connected with the entrance of first gas-liquid separator 9；Wherein, first cooler 8 is specially that carbon dioxide produces
Product Gas Cooler.
In order to which the liquid reflux of isolating the first gas-liquid separator 9 is into desorber 6, the desorber unit further includes
The entrance of reflux pump 12, the reflux pump 12 is gone out by condensate return pipeline 11 and the liquid phase of first gas-liquid separator 9
Mouth is connected, and the outlet of the reflux pump 12 is connected with the reflux water inlet of the desorber 6；Wherein, the reflux pump 12 is specific
For condensate return pump.
In order to which the poor amine liquid for desorbing tower bottom is delivered in First Heat Exchanger 4, the desorber unit further include: second
The entrance of circulating pump 13, second circulation pump 13 is connected with 6 bottom of desorber, the second circulation pump 13 outlet and
The second end entrance (poor amine liquid entrance) of the First Heat Exchanger 4 is connected；Wherein, the second circulation pump 13 is specially poor amine
Liquid circulating pump.
Described hydrogen recovery unit one end is connected with the top exit on the absorption tower 2,24 phase of the other end and PSA unit
Even, the hydrogen recovery unit is used to the carbon monoxide in the periodic off-gases purified gas being changed into carbon dioxide, becomes in generation
Gas exports hydrogen product and the 2nd PSA periodic off-gases after 24 pressure-variable adsorption of PSA unit.
Here, referring to Fig. 1, the hydrogen recovery unit includes:
Compressor 16, the entrance of the compressor 16 are connected with the top exit on the absorption tower 2, for compressing described speed
Deflation purified gas, to meet the requirement of shift-converter 22 and PSA unit 24 to pressure；
Second gas-liquid separator 18, the entrance of second gas-liquid separator 18 are connected with the outlet of the compressor 16,
For the compressed periodic off-gases purified gas of gas-liquid separation；
Second heat exchanger 20, first end (the compression purification gas side) entrance of second heat exchanger 20 and second gas-liquid
The gaseous phase outlet of separator 18 is connected, the middle change gas and gas-liquid that second heat exchanger 20 is used to generate using shift-converter 22
The periodic off-gases purified gas after separation exchanges heat, to heat up to periodic off-gases purified gas；Wherein, second heat exchanger
20 be specially the compression middle change gas heat exchanger of purified gas-, has the beneficial effect for the energy consumption that recovers energy, reduces.
(compression is net for the first end of shift-converter 22, the entrance of the shift-converter 22 and second heat exchanger 20
Change gas side) outlet is connected, and for making the reaction of carbon monoxide in the periodic off-gases purified gas become carbon dioxide, the transformation is anti-
The outlet of device 22 is answered to be connected with second end (middle change gas side) entrance of second heat exchanger 20, the of the shift-converter 22
Two ends (middle change gas side) outlet is connected with PSA unit 24, after the processing of PSA unit 24, exports hydrogen by hydrogen output channel 25
Product exports the second periodic off-gases by the second periodic off-gases output channel 26.Wherein, the middle change gas refers in shift-converter 22
React the gas generated.
Here, in order to cool down to compressed periodic off-gases purified gas, the hydrogen recovery unit further includes that third is cold
But device 17, the entrance of the third cooler 17 are connected with the outlet of the compressor 16, the outlet of the third cooler 17
It is connected with the entrance of second gas-liquid separator 18.Wherein, the third cooler 17 is specially to compress purification Gas Cooler.
In order to which the periodic off-gases purified gas after heat exchanging further heats, to reach reaction temperature, the hydrogen recovery unit
It further include heater 21, the entrance of the heater 21 is connected with the outlet of the first end of second heat exchanger 20, the heating
The outlet of device 21 is connected with the entrance of the shift-converter 22；
In order to which the middle change gas generated to reaction further cools down, the hydrogen recovery unit further includes the 4th cooler 23,
The entrance of 4th cooler 23 is connected with the outlet of the second end of second heat exchanger 20 (middle change gas exports), and the described 4th
The outlet of cooler 23 is connected with the entrance of the PSA unit 24；Wherein, the 4th cooler 23 is specially middle change air cooling
Device.
Further, described device further includes liquid knockout 15, is gone out at the top of the entrance of the liquid knockout 15 and the absorption tower 2
Mouth is connected, and the first outlet (bottom) of the liquid knockout 15 is connected with the liquid return hole (top) on the absorption tower 2, the liquid knockout
15 second outlet (top) is connected with the entrance of the compressor 16, and the liquid knockout 15 is for removing in periodic off-gases purified gas
Free water.Wherein, periodic off-gases purified gas is entered in liquid knockout 15 by 2 tower top of absorption tower, enters compressor after removing free water
It is compressed in 16；Free water is returned in absorption tower 2 by 15 bottom of liquid knockout.The purpose that liquid knockout 15 is arranged is to remove periodic off-gases
The free water and unhindered amina liquid carried in purified gas has and reduces the loss of amine liquid, reduces having for rear end hydrogen recycling energy consumption simultaneously
Beneficial effect.
Further, in order to which the rich amine solution of absorb the bottom of the tower to be delivered in First Heat Exchanger, described device further include: the
The entrance of one circulating pump 3, the first circulation pump 3 is connected with 2 outlet at bottom of absorption tower, and the first circulation pump 3 goes out
Mouth is connected with the first end (rich amine solution entrance) of the First Heat Exchanger 4；Wherein, the first circulation pump 3 is specially rich amine solution
Circulating pump.
In order to make the poor amine liquid of desorber tower bottom be down to predetermined temperature, described device before flowing back to absorption tower further include:
The second end outlet of second cooler 14, the entrance of second cooler 14 and the First Heat Exchanger 4 (poor amine liquid exports)
It is connected, the outlet of second cooler 14 is connected with the top entry on the absorption tower 2；Wherein, second cooler 14
Specially poor amine liquid cooler, for further cooling down to the poor amine liquid after First Heat Exchanger heat exchange cooling.
Further, enter suitable flow in desorber to adjust rich amine solution, improve the desorption efficiency of carbon dioxide, join
See Fig. 1, described device further includes return line 5, and one end of the return line 5 is connected to the outlet of the first circulation pump 3
On pipeline between the first end entrance (rich amine solution entrance) of the First Heat Exchanger 4, the other end of the return line 5
The pipe being connected between the second end outlet (poor amine liquid outlet) of the First Heat Exchanger 4 and the entrance of second cooler 14
On line.Wherein, the return line 5 is specially rich amine solution return line, excessive rich amine solution by return line 5 with self solve
The poor amine liquid for inhaling tower 6 is mixed, is transported in absorption tower 2 again after cooling, continues heat and mass with the first PSA periodic off-gases, to protect
Demonstrate,prove the carbon dioxide saturation degree of 2 tower bottom rich amine solution of absorption tower.
Further, in order to which the condensed water that the second gas-liquid separator separates go out is discharged, described device further includes drainpipe 19,
The drainpipe 19 is connected with the gaseous phase outlet of second gas-liquid separator 18, and the drainpipe 19 is for discharging the second gas-liquid
Separator 18 isolates the condensed water in compression purified gas.
Through the above as can be seen that the embodiment of the present application is raw to the first PSA periodic off-gases decarburization by absorption tower unit
At rich amine solution and periodic off-gases purified gas, rich amine solution enters desorber unit after First Heat Exchanger exchanges heat and is desorbed, and isolates
Carbon dioxide；In addition, periodic off-gases purified gas further extracts hydrogen therein through PSA unit after entering hydrogen recovery unit reaction
Gas, to improve hydrogen recovery rate.
The utility model is described further below by hydrogen making by natural gas reformation periodic off-gases recovery method.
A kind of hydrogen making by natural gas reformation periodic off-gases recovery method, as shown in Figure 2, comprising the following steps:
The S110: the one PSA periodic off-gases of step enter in absorption tower 2 through the first periodic off-gases output channel 1, absorption tower 2
Carbon dioxide in first PSA periodic off-gases described in interior poor amine absorption generates rich amine solution and periodic off-gases purified gas；
Step S120: the rich amine solution flows out and is divided into two-way by 2 tower bottom of absorption tower, changes wherein entering first all the way
Enter desorber unit after hot device 4, with the poor amine liquid heat exchange heating from desorber unit, another way flows into return line 5；
Specifically, the rich amine solution is flowed out by 2 tower bottom of absorption tower is divided into two-way after 3 pressurization of first circulation pump,
A part enters desorber 6 after transporting to First Heat Exchanger 4 and the heat exchange heating of poor amine liquid；A part is back to by return line 5
Absorption tower 2, to guarantee the carbon dioxide saturation degree of tower bottom rich amine solution.
Step S130: into the rich amine solution of desorber unit, in desorber unit after air lift carbon dioxide, desorption
Poor amine liquid afterwards is after the First Heat Exchanger 4 cools down with rich amine solution heat exchange, after mixing with the rich amine solution in the return line 5
It reenters in the absorption tower 2 for absorbing carbon dioxide in first periodic off-gases；The dioxy that desorber unit desorbs
Change carbon, carbon dioxide product gas is obtained after the first gas-liquid separator 9 isolates free water；
Specifically, rich amine solution enters desorber 6, in desorber 6 after air lift carbon dioxide, in tower bottom reboiler
In 7 after heat penetration decarburization, the poor amine liquid of generation transports to First Heat Exchanger 4 and rich amine solution heat exchange cools down through second circulation pump 13
Afterwards, mixed with the rich amine solution in the return line 5, and after the second cooler 14 is cooled to predetermined temperature, again into
Enter in the absorption tower 2 for absorbing carbon dioxide in first periodic off-gases；The carbon dioxide desorbed in desorber 6, warp
It crosses after the first cooler 8 cools down to enter after the first gas-liquid separator 9 isolates free water and obtains carbon dioxide product gas；Wherein,
First gas-liquid separator 9 carries out gas-liquid separation to the carbon dioxide desorbed, and the condensed water isolated is back to through reflux pump 12
In desorber 6, the carbon dioxide product gas after separation passes through CO2Output channel 10 exports.
Step S140: the periodic off-gases purified gas is through entering hydrogen recovery unit at the top of the absorption tower 2, by the hydrogen
Carbon monoxide in the periodic off-gases purified gas is changed into carbon dioxide by gas recovery unit, becomes gas, the middle change gas in generation
Hydrogen product and the 2nd PSA periodic off-gases are discharged after the processing of PSA unit 24.
Specifically, the periodic off-gases purified gas removes free water through entering liquid knockout 15 at the top of the absorption tower 2, then
It is compressed through compressor 16, carries out gas-water separation, the condensed water elimination isolated to drainpipe using the second gas-liquid separator 18
19, the compression purified gas isolated heats up by the second heat exchanger 20 and the heat exchange of middle change gas, further heats into heater 21
To conversion reaction temperature, into reacting in shift-converter 22, the carbon monoxide compressed in purified gas is changed into titanium dioxide
Carbon, the middle change gas of generation is after second heat exchanger 20 cools down with compression purified gas heat exchange, into the 4th cooler 23
Further cooling, the middle change gas after cooling enters PSA unit 24, the hydrogen product generated after the PSA unit 24 processing by
Hydrogen output channel 25 is discharged, and the second periodic off-gases (as fuel) of generation are discharged by the second periodic off-gases output channel 26.Second
For off-gas compared with the first off-gas, hydrogen therein and carbon dioxide have obtained abundant recycling.
It should be noted that step S120, step S130, step S140 can be carried out simultaneously.
The hydrogen making by natural gas reformation periodic off-gases recyclable device of the application can effectively recycle hydrogen making by natural gas reformation PSA and speed to put
Carbon dioxide and hydrogen in gas, for the purity of carbon dioxide up to 99% or more, the rate of recovery is higher than 80%；The purity of hydrogen reaches
99% or more, hydrogen entirety recovery rate is up to 80% or more.
It should be noted last that the above specific embodiment is only to illustrate the technical solution of the utility model rather than limits
System, although the utility model is described in detail referring to example, those skilled in the art should understand that, it can be right
The technical solution of the utility model is modified or replaced equivalently, without departing from the spirit and model of technical solutions of the utility model
It encloses, should all cover in the scope of the claims of the utility model.
Claims (9)
1. a kind of hydrogen making by natural gas reformation periodic off-gases recyclable device characterized by comprising
Absorption tower, the unstripped gas entrance on the absorption tower are connected with the first periodic off-gases output channel, are used for the first PSA periodic off-gases
In carbon dioxide and the poor amine liquid in the absorption tower react and generate rich amine solution and periodic off-gases purified gas；
First end entrance of First Heat Exchanger, the First Heat Exchanger is connected with absorb the bottom of the tower outlet, and described first changes
Hot device using the poor amine liquid in desorber unit with the rich amine solution for being exchanged heat；
The first end of desorber unit, the desorber unit is connected with the outlet of the first end of the First Heat Exchanger, the solution
The second end for inhaling tower unit is connected with the second end entrance of the First Heat Exchanger, the second end of the First Heat Exchanger export and
The top entry on the absorption tower is connected, the desorber unit for being desorbed to the rich amine solution, obtain poor amine liquid and
Carbon dioxide；
Hydrogen recovery unit, described hydrogen recovery unit one end is connected with the top exit on the absorption tower, the other end and PSA are mono-
Member is connected, and the hydrogen recovery unit is used to the carbon monoxide in the periodic off-gases purified gas being changed into carbon dioxide, generates
Middle change gas exports hydrogen product and the 2nd PSA periodic off-gases after the PSA unit pressure-variable adsorption.
2. hydrogen making by natural gas reformation periodic off-gases recyclable device as described in claim 1, which is characterized in that the desorber unit
Include:
Desorber, the inlet of the desorber are connected with the outlet of the first end of the First Heat Exchanger, the bottom of the desorber
Portion outlet is connected with the second end entrance of the First Heat Exchanger, for carrying out air lift carbon dioxide removal to the rich amine solution；
Reboiler, the reboiler are connected with the bottom of the desorber, for further to the rich amine solution decarburization；
First gas-liquid separator, first gas-liquid separator are connected with the top exit of the desorber, are used for gas-liquid separation
The carbon dioxide is obtained after free water out.
3. hydrogen making by natural gas reformation periodic off-gases recyclable device as claimed in claim 2, which is characterized in that the desorber unit
Further include:
The entrance of first cooler, first cooler is connected with the top exit of the desorber, first cooler
Outlet be connected with the entrance of first gas-liquid separator；
Reflux pump, the entrance of the reflux pump are connected with the liquid-phase outlet of first gas-liquid separator, and the reflux pump goes out
Mouth is connected with the reflux water inlet of the desorber.
4. hydrogen making by natural gas reformation periodic off-gases recyclable device as described in claim 1, which is characterized in that the hydrogen recycling is single
Member includes:
Compressor, the entrance of the compressor are connected with the top exit on the absorption tower, for compressing the periodic off-gases purification
Gas；
The entrance of second gas-liquid separator, second gas-liquid separator is connected with the outlet of the compressor, for gas-liquid point
From the periodic off-gases purified gas；
Second heat exchanger, the first end entrance of second heat exchanger are connected with the gaseous phase outlet of second gas-liquid separator,
Second heat exchanger be used for using shift-converter generate middle change gas and gas-liquid separation after the periodic off-gases purified gas into
Row heat exchange；
Shift-converter, the entrance of the shift-converter are connected with the outlet of the first end of second heat exchanger, are used for institute
It states the carbon monoxide in periodic off-gases purified gas and is changed into carbon dioxide, the outlet of the shift-converter and second heat exchanger
The second end entrance be connected, the outlet of the second end of the shift-converter is connected with PSA unit.
5. hydrogen making by natural gas reformation periodic off-gases recyclable device as claimed in claim 4, which is characterized in that the hydrogen recycling is single
Member further includes third cooler, and the entrance of the third cooler is connected with the outlet of the compressor, the third cooler
Outlet be connected with the entrance of second gas-liquid separator.
6. hydrogen making by natural gas reformation periodic off-gases recyclable device as claimed in claim 4, which is characterized in that the hydrogen recycling is single
Member further include:
Heater, the entrance of the heater are connected with the outlet of the first end of second heat exchanger, the outlet of the heater
It is connected with the entrance of the shift-converter；
The entrance of 4th cooler, the 4th cooler is connected with the outlet of the second end of second heat exchanger, and the described 4th
The outlet of cooler is connected with the entrance of the PSA unit.
7. the hydrogen making by natural gas reformation periodic off-gases recyclable device as described in one of claim 4-6, described device further includes except liquid
Device,
The entrance of the liquid knockout is connected with the absorption tower top exit, the first outlet of the liquid knockout and the absorption tower
Liquid return hole be connected, the second outlet of the liquid knockout is connected with the entrance of the compressor.
8. the hydrogen making by natural gas reformation periodic off-gases recyclable device as described in one of claim 1-6, which is characterized in that described device
Further include:
The entrance of first circulation pump, the first circulation pump is connected with absorb the bottom of the tower outlet, the first circulation pump
Outlet is connected with the first end of the First Heat Exchanger；
The entrance of second cooler, second cooler is connected with the outlet of the second end of the First Heat Exchanger, and described second
The outlet of cooler is connected with the top entry on the absorption tower.
9. hydrogen making by natural gas reformation periodic off-gases recyclable device as claimed in claim 8, which is characterized in that described device further includes
Return line,
One end of the return line is connected to outlet and the first end entrance of the First Heat Exchanger of the first circulation pump
Between pipeline on；The second end that the other end of the return line is connected to the First Heat Exchanger exports and described second is cold
But on the pipeline between the entrance of device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820857450.6U CN208561684U (en) | 2018-06-04 | 2018-06-04 | Hydrogen making by natural gas reformation periodic off-gases recyclable device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820857450.6U CN208561684U (en) | 2018-06-04 | 2018-06-04 | Hydrogen making by natural gas reformation periodic off-gases recyclable device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN208561684U true CN208561684U (en) | 2019-03-01 |
Family
ID=65484425
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820857450.6U Active CN208561684U (en) | 2018-06-04 | 2018-06-04 | Hydrogen making by natural gas reformation periodic off-gases recyclable device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN208561684U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108622856A (en) * | 2018-06-04 | 2018-10-09 | 新疆敦华石油技术股份有限公司 | Hydrogen making by natural gas reformation periodic off-gases retracting device and recovery method |
-
2018
- 2018-06-04 CN CN201820857450.6U patent/CN208561684U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108622856A (en) * | 2018-06-04 | 2018-10-09 | 新疆敦华石油技术股份有限公司 | Hydrogen making by natural gas reformation periodic off-gases retracting device and recovery method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102985161B (en) | The separation equipment and process thereof of producing gases at high pressure is purged by gas pressurized | |
| CN103523751A (en) | Device and method for performing cryogenic separation and purification on carbon monoxide and hydrogen | |
| CN102977960A (en) | Process for co-producing and synthetic natural gas and food-grade carbon dioxide by using calcium carbide furnace gas | |
| CN113277471A (en) | Method and device for recovering reduction tail gas in polycrystalline silicon production | |
| CN102413901A (en) | Apparatus and method for compressing co2, system and method for separating and recovering co2 | |
| CN208561684U (en) | Hydrogen making by natural gas reformation periodic off-gases recyclable device | |
| CN104987279A (en) | Methanol-making system and method through coal gasification integrating waste heat cooling and carbon trapping | |
| CN104986734A (en) | Synthesis ammonia and synthesis gas self-circulation cryogenic separation purifying device and purifying method thereof | |
| CN109232161A (en) | In a kind of power-plant flue gas carbon dioxide recovery with utilize system and method | |
| CN211688249U (en) | CO before large-scale combustion2Trapping system | |
| CN108622856A (en) | Hydrogen making by natural gas reformation periodic off-gases retracting device and recovery method | |
| JP5736916B2 (en) | Method for recovering and liquefying carbon dioxide from mixed gas | |
| JPH0449029B2 (en) | ||
| CN212842469U (en) | Single-tower cryogenic rectification argon recovery system with argon circulation and hydrogen circulation | |
| CN111977654B (en) | CO is retrieved in low temperature methanol washing workshop section2Is a device and process thereof | |
| CN211716983U (en) | Device for separating and purifying krypton and xenon | |
| CN212842470U (en) | Single-tower cryogenic rectification argon recovery system with circulation function | |
| CN204752197U (en) | Synthetic ammonia synthetic gas self -loopa cryogenic separation purifier | |
| CN204939342U (en) | The gasification methyl alcohol system of a kind of integrated utilizing waste heat for refrigeration and carbon trapping | |
| US7461521B2 (en) | System unit for desorbing carbon dioxide from methanol | |
| CN104108689B (en) | One utilizes Ammoximation reaction emptying end gas to extract nitric oxide production method and device | |
| CN210410096U (en) | Separation system for carbon dioxide in medium-high pressure gas source | |
| CN102757016B (en) | Method and device for cogeneration of synthesis ammonia gas and liquefied natural gas prepared through pressure gasification of crushed coal in fixed bed | |
| RU2760013C2 (en) | Method and installation for the formation of synthesis gas | |
| CN111637684A (en) | Single-tower cryogenic rectification argon recovery system with circulation and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 834000 second floor, No. 77, Nanxin Road, Karamay District, Karamay City, Xinjiang Uygur Autonomous Region Patentee after: Xinjiang Dunhua Green Carbon Technology Co.,Ltd. Address before: No. 69-13-11, Yingbin Avenue, Karamay, Xinjiang Uygur Autonomous Region 834000 Patentee before: XINJIANG DUNHUA PETROLEUM TECHNOLOGY CO.,LTD. |
|
| CP03 | Change of name, title or address |