CN105502289B - The separation method and its system of hydrogen in a kind of catalytic cracked dry gas - Google Patents
The separation method and its system of hydrogen in a kind of catalytic cracked dry gas Download PDFInfo
- Publication number
- CN105502289B CN105502289B CN201410495746.4A CN201410495746A CN105502289B CN 105502289 B CN105502289 B CN 105502289B CN 201410495746 A CN201410495746 A CN 201410495746A CN 105502289 B CN105502289 B CN 105502289B
- Authority
- CN
- China
- Prior art keywords
- hydrate
- hydrogen
- dry gas
- entrance
- section
- 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.)
- Expired - Fee Related
Links
- 239000007789 gas Substances 0.000 title claims abstract description 105
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 61
- 239000001257 hydrogen Substances 0.000 title claims abstract description 61
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 61
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 56
- 238000000926 separation method Methods 0.000 title claims abstract description 54
- 238000006703 hydration reaction Methods 0.000 claims abstract description 65
- 230000036571 hydration Effects 0.000 claims abstract description 50
- 239000012224 working solution Substances 0.000 claims abstract description 34
- 238000000034 method Methods 0.000 claims abstract description 22
- 230000008569 process Effects 0.000 claims abstract description 12
- 230000003472 neutralizing effect Effects 0.000 claims description 15
- 239000002002 slurry Substances 0.000 claims description 15
- 238000004523 catalytic cracking Methods 0.000 claims description 5
- 238000005336 cracking Methods 0.000 claims description 4
- 230000008859 change Effects 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 9
- 150000002431 hydrogen Chemical class 0.000 abstract 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 11
- 239000005977 Ethylene Substances 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 9
- 238000010521 absorption reaction Methods 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 239000000243 solution Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- JRMUNVKIHCOMHV-UHFFFAOYSA-M tetrabutylammonium bromide Chemical compound [Br-].CCCC[N+](CCCC)(CCCC)CCCC JRMUNVKIHCOMHV-UHFFFAOYSA-M 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- FPGGTKZVZWFYPV-UHFFFAOYSA-M tetrabutylammonium fluoride Chemical compound [F-].CCCC[N+](CCCC)(CCCC)CCCC FPGGTKZVZWFYPV-UHFFFAOYSA-M 0.000 description 2
- 241000628997 Flos Species 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000000887 hydrating effect Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The present invention provides the separation method and its system of hydrogen in a kind of catalytic cracked dry gas, which includes making catalytic cracked dry gas that hydration reaction occur, and collect the process of hydrogen-rich gas, wherein, realize that the hydration reactor of hydration reaction has following structure：Hydration reactor cavity has entrance, trunnion section and stable section along hydrate working solution flow direction, and the circulation area of trunnion section is respectively less than the circulation area of entrance and stable section, and the side wall which corresponds to trunnion section offers air inlet.The separation method of hydrogen, which does not need to hydrogen in existing hydrate separation method separation catalytic cracked dry gas, in catalytic cracked dry gas provided by the invention needs to compress the step of boosting to catalytic cracked dry gas, has the advantages that operation is reliable, practical application in industry feasibility is strong.
Description
Technical field
The present invention relates to the separation methods and its system of hydrogen in a kind of catalytic cracked dry gas, belong to chemical technology field.
Background technology
Due to containing a large amount of hydrogen and ethylene in catalytic cracked dry gas, it can be annual to their comprehensive utilization
Millions of ton of ethylene cracking material and hydrogen feedstock is saved, there is billions of economic benefits.In recent years, many researchers
Separation and recycling to hydrogen in catalytic cracked dry gas and ethylene have carried out a large amount of research, are currently used for separation catalytic cracking and do
The method of hydrogen and ethylene has separation by deep refrigeration, absorption and separation method, membrane separation process and hydrate separation method in gas.However above-mentioned side
Method but there are it is different the defects of, constrain the recycling of hydrogen and ethylene in catalytic cracked dry gas.
For example, the shortcomings that although cold separation technology is more mature, and energy consumption is higher but restricts the technology always
It promotes and applies, generally only in the more area of the larger refinery for the treatment of capacity, oil catalytic cracking unit or oil refining-chemical industry
Integration firm can just consider to detach catalytic cracked dry gas using cold separation technology；Membrane separation process is also located in terms of ethylene extraction
It in conceptual phase, since the film that separation uses easily is influenced by impurity and damages, while in the presence of being film-made, cost is higher to ask again
Topic, so as to fail to be widely used always；Absorption and separation method have it is simple for process, equipment and materials is common, operating condition temperature
With and the advantages of low energy consumption, efficient, but be typically only capable to the gas of processing low concentration, and the removing of impurity is relatively difficult.
Absorption and separation method can be divided into Physical Absorption and chemical absorbing in the way of absorption.Wherein, the typical technology in Physical Absorption method
It is cold oil absorption process, which is to detach the traditional technology of ethylene in catalytic cracked dry gas, adaptable strong, investment
The advantages of expense is low, process scale is small, but the technique there are high energy consumption, ethylene loss amount is big the defects of；Chemical absorption method is called π
Absorptive complex wave isolation technics, this method have that absorptive capacity is big, the advantages of Recovery rate of ethylene is high, but commercial Application and few at present
See.
Hydrate separation method is a kind of isolation technics of new separation low boiling point mixed gas, and principle is according to gas with various
The complexity of hydrate is formed, so as to fulfill the separation of each component in mixed gas.Relative to above-mentioned gas partition method, hydration
The advantage of object partition method is that condition is milder, and the separation and purification of mixed gas, nothing can be realized between 0-15 DEG C of temperature
Still all there is apparent advantage in equipment investment by energy consumption.However, the prior art is detached using hydrate separation method
Hydrogen and during ethylene in catalytic cracked dry gas, usually will to implementing compression boosting processing as the catalytic cracked dry gas of unstripped gas,
It is then fed into gas hydrate reactor and is mixed with hydrate working solution.It is limited to execute-in-place space and gas compressor
The reason of energy consumption etc., at present hydrate separation technology not yet obtained in terms of the hydrogen in detaching catalytic cracked dry gas extensively
Using.Therefore, the hydrogen in new hydrate separation catalytic cracked dry gas is studied, it is of interest by researcher always.
Invention content
Technical problem solved by the invention is, provides the separation method of hydrogen in a kind of catalytic cracked dry gas and its is
System, this method, which does not need to hydrogen in existing hydrate separation method separation catalytic cracked dry gas, to be needed to compress liter to catalytic cracked dry gas
The step of pressure, has the advantages that operation is reliable, practical application in industry feasibility is strong.
The present invention provides a kind of separation method of hydrogen in catalytic cracked dry gas, including making catalytic cracked dry gas that water occur
Reaction is closed, and collects the process of hydrogen-rich gas, wherein,
Realize that the hydration reactor of hydration reaction has following structure：Hydration reactor cavity is flowed along hydrate working solution
Direction has entrance, trunnion section and stable section, and the circulation area of trunnion section is respectively less than the circulating face of entrance and stable section
Product, the side wall which corresponds to trunnion section offer air inlet；
The separation method includes：Hydrate working solution is sent into from entrance in the hydration reactor, splits catalysis
Change dry gas to connect with hydration reactor by air inlet, will be treated point using the suction for the hydrate working solution generation for flowing through trunnion section
Hydration reactor is sucked from catalytic cracked dry gas, and the two is made to be mixed during stable section is flow to and hydration reaction occurs,
Generate hydrate slurry and hydrogen-rich gas；
The hydrate slurry and hydrogen-rich gas are sent into hydrate separator, detaches and collects hydrogen-rich gas.
The separation method of hydrogen in above-mentioned catalytic cracked dry gas, is mainly utilized hydromechanical principle, utilizes hydrate
The flowing of different location of the working solution in hydration reactor and the changing rule of pressure, realize the suction of catalytic cracked dry gas
Enter, the process from boosting and hydration separation.It is in particular in：Hydrate working solution is noted from the entrance of hydration reactor
Enter, when it reaches the trunnion section of hydration reactor, since actual internal area drastically reduces, so as to which its flow velocity be made to increase suddenly,
The static pressure in hydration reactor is made quickly to reduce, under the action of pressure differential, catalytic cracked dry gas has been inhaled into hydration reactor
In mixed with hydrate working solution, when catalytic cracked dry gas and hydrate working solution reach the stable section of hydration reactor, by
In the expansion of actual internal area, so as to increase the static pressure of fluid, the pressure of system enters hydration instead higher than catalytic cracked dry gas
The pressure of device is answered, when the static pressure of fluid is more than the generation pressure of hydrate, methane, ethane, ethylene in catalytic cracked dry gas
Hydration reaction occurs with the components such as carbon dioxide and hydrate working solution, forms hydrate slurry, and institute in catalytic cracked dry gas
A part of gas phase of hydrogen obtains enrichment and forms hydrogen-rich gas.
In the specific embodiment of the present invention, make the hydrogen-rich gas from the discharge of the top exit of hydrate separator and
It is collected, outlet at bottom of the hydrate slurry through hydrate separator is sent into hydrate neutralizing device and implements neutralizing, neutralizing
The hydrate working solution of removing gas gone out is used for hydration reaction cycle.
In the specific embodiment of the present invention, temperature when making the hydrate working solution enter hydration reactor is 4-15
DEG C, pressure 1.0-5.1MPa.Hydrate working solution under the temperature and pressure is more advantageous to flowing through trunnion section formation pressure at it
Force difference so as to be conducive to the stable section that cracking catalysis dry gas is inhaled into hydration reactor, is allowed to carry out water with hydrate working solution
Reaction is closed, forms hydrate slurry.
In the specific embodiment of the present invention, the internal diameter of the pipeline of the entrance of the hydration reactor is 15-50mm, institute
It is 0.05-0.5, the diameter of the air inlet and the trunnion that the internal diameter of trunnion section, which is stated, with the internal diameter of the pipeline ratio of the entrance
The internal diameter ratio of section is 0.2-0.5；
The internal diameter of the pipeline ratio of the length of the entrance and the entrance is 1-3, the trunnion segment length with it is described
The ratio of trunnion section internal diameter is 1-2.5, and the internal diameter of the pipeline ratio of the length of the stable section and the entrance is 3-5.
In the specific embodiment of the present invention, the operation temperature of the hydrate separator is 4-15 DEG C, operating pressure
For 1.1-5.1MPa.Control aforesaid operations temperature and operating pressure that can make hydrate slurry and catalysis in hydrate separator
Hydrogen in cracking dry gas detaches the separation for realizing gas phase and liquid phase completely as far as possible.
In the specific embodiment of the present invention, the operation temperature of the hydrate neutralizing device is 8-23 DEG C, operating pressure
For 0.1-2.1MPa.Control aforesaid operations temperature and pressure can make hydrate slurry complete as far as possible in hydrate dissolves device
Full neutralizing obtains hydrogen depleted gas and hydrate working solution, realizes the separation of hydrogen depleted gas and hydrate working solution.
In the specific embodiment of the present invention, catalytic cracked dry gas to be separated is inhaled into the pressure before hydration reactor and is
0.6-1.6MPa。
The present invention also provides the system for realizing the separation method of hydrogen in above-mentioned catalytic cracked dry gas, the system comprises
Hydrate work liquid storage tank, hydration reactor, hydrate separator, hydrate neutralizing device, heater and/or pressure reducing valve；
Wherein, hydration reactor cavity has entrance, trunnion section and stable section along hydrate working solution flow direction, and
The circulation area of trunnion section is respectively less than the circulation area of entrance and stable section, which corresponds to trunnion section
Side wall offers air inlet；
The hydrate work liquid storage tank is equipped with entrance and exit, the outlet of the hydrate work liquid storage tank and the water
Close the entrance connection of reactor；
The hydration reactor stable section is equipped with the outlet for discharging hydrate slurry and hydrogen-rich gas, with the water
The entrance connection of object separator is closed, the top of the hydrate separator is equipped with hydrogen-rich gas floss hole, and bottom is equipped with hydrate
Serum outlet；
The hydrate slurry outlet of the hydrate separator connects, and set between the two with the entrance of hydrate neutralizing device
Having heaters and/or pressure reducing valve, the hydrate working solution outlet of the removing gas of the hydrate neutralizing device and the hydrate
The entrance connection of work liquid storage tank.
In above system, the internal diameter of the pipeline of the entrance of the hydration reactor is 15-50mm, the trunnion section it is interior
The internal diameter of the pipeline ratio of diameter and the entrance is 0.05-0.5, the diameter of the air inlet and the internal diameter ratio of the trunnion section
For 0.2-0.5；
The internal diameter of the pipeline ratio of the length of the entrance and the entrance is 1-3, the trunnion segment length with it is described
The internal diameter ratio of trunnion section is 1-2.5, and the internal diameter of the pipeline ratio of the length of the stable section and the entrance is 3-5.
The separation method of hydrogen in catalytic cracked dry gas provided by the invention, employs structually improved hydration reactor,
Dexterously change by circulation area in hydration reactor and the required hydrating condition of catalytic cracked dry gas (hydration generation pressure is provided
Power), that is, pressure drop caused by trunnion section (even up to parital vacuum) is being flowed through by catalytic cracking using hydrate working solution
After dry gas sucking hydration reactor, and due to pressure increase and the two filling under pressure-driven during stable section is flowed to
Divide and mix and the components such as the alkane and alkene in catalytic cracked dry gas is promoted all to be hydrated as far as possible, reach separation hydrogen
Purpose.Compared to the technique detached at present to catalytic cracked dry gas, separation method of the invention is not needed to to be separated
Catalytic cracked dry gas carries out compression boosting, not only eliminates the input of compression device, significantly reduces energy consumption, during hydration reaction
Without additional rabbling mechanism, and the requirement to operating space and operational sequence all significantly reduces, and realizes catalytic cracking and does
The separation of hydrogen in gas, the industrial applications for the technology provide possibility.
Description of the drawings
Fig. 1 is the process flow chart of hydrogen in present invention separation catalytic cracked dry gas.
Fig. 2 is the hydration reactor in hydrogen gas system in present invention separation catalytic cracked dry gas.
Reference numeral：
1- hydrates work liquid storage tank；2- hydration reactors；3- hydrate separators；4- hydrates dissolve device；5- high pressures
Pump；6- coolers；7- heaters；8- pressure reducing valves；9- hydrate working solutions；10- catalytic cracked dry gas；
01- entrances；02- trunnion sections；03- expanding reach；04- air inlets.
Specific embodiment
Purpose, technical scheme and advantage to make the embodiment of the present invention are clearer, below in the embodiment of the present invention
Technical solution is clearly and completely described, it is clear that described embodiment is part of the embodiment of the present invention rather than complete
The embodiment in portion.Based on the embodiments of the present invention, those of ordinary skill in the art are without making creative work
All other embodiments obtained shall fall within the protection scope of the present invention.
The separation method of hydrogen in catalytic cracked dry gas of the present invention, including making catalytic cracked dry gas that hydration reaction occur, and
The process of hydrogen-rich gas is collected, wherein,
Realize the hydration reactor of hydration reaction as shown in Fig. 2, having following structure：Hydration reactor cavity is along hydrate
Working solution flow direction has entrance 01, trunnion section 02 and stable section 03, and the circulation area of trunnion section 02 is respectively less than entrance
The circulation area of section 01 and stable section 03, the side wall which corresponds to trunnion section 02 offer air inlet 04；
Wherein, the internal diameter of the pipeline of the entrance 01 of hydration reactor is 15-50mm, in the internal diameter of trunnion section 02 and the pipeline of entrance 01
Diameter ratio is 0.05-0.5, and the diameter of air inlet 04 is 0.2-0.5 with the internal diameter ratio of trunnion section 02；The length of entrance 01 with
The internal diameter of the pipeline ratio of entrance 01 is 1-3, and the internal diameter ratio of 02 length of trunnion section and trunnion section 02 is 1-2.5, stable section 03
The internal diameter of the pipeline ratio of length and entrance 01 be 3-5.
As shown in Figure 1, the separation method of hydrogen includes in catalytic cracked dry gas of the present invention：By hydrate work liquid storage tank 1
In hydrate working solution 9 after high-pressure pump 5 and cooler 6, from entrance 01 be sent into hydration reactor 2 in, make hydrate work
The temperature made when liquid 9 enters hydration reaction 2 is 4-15 DEG C, pressure 1.0-5.1MPa.Catalytic cracked dry gas 10 is made to pass through air inlet
Mouth 04 is connected with hydration reactor 2, and catalytic cracked dry gas 10 to be separated is inhaled into the pressure 0.6- before hydration reactor 2
Catalytic cracked dry gas 10 to be separated is sucked water by 1.6MPa, the suction generated using the hydrate working solution 9 for flowing through trunnion section 02
Reactor 2 is closed, and the two is made to be mixed during stable section 03 is flow to and hydration reaction occurs, generates hydrate slurry and richness
Hydrogen；
Hydrate slurry and hydrogen-rich gas are sent into hydrate separator 3, the operation temperature of hydrate separator 3 is 4-15
DEG C, operating pressure 1.1-5.1Mpa is detached and is collected hydrogen-rich gas.
Hydrogen-rich gas is made to be collected from the top exit discharge of hydrate separator 3, by hydrate slurry through hydrate
The outlet at bottom of separator 3 is sent into hydrate neutralizing device 4 after heated device 7 and pressure reducing valve 8 and implements neutralizing, hydrate neutralizing device 4
Operation temperature for 8-23 DEG C, operating pressure 0.1-2.1Mpa, dissolve the hydrate working solution of removing gas and return to water
It closes in object working liquid tank 1 and is used for hydration reaction cycle.
In the present invention, hydrate working solution selection can according to the height of each component concentration in catalytic cracked dry gas and
Selection can be the aqueous solution of tetrabutylammonium bromide or tetrabutyl ammonium fluoride or be added to and can improve hydrate
Other chemical substances of formation speed, these substances add in whether and concentration height do not influence the present invention technical side
Case.
Embodiment 1
Hydrate working solution is tetrabutylammonium bromide (english abbreviation：TBAB), a concentration of 10wt%；
The composition of catalytic cracked dry gas is as shown in table 1 below：
The composition of 1 catalytic cracked dry gas of table
| Composition | CH4 | C2H6 | C2H4 | C3H6 | CO2 | H2 |
| Content, mol% | 23.79 | 7.65 | 21.61 | 0.24 | 2.85 | 44.86 |
Using the technological process of hydrogen and the hydration reactor of Fig. 2 in separation catalytic cracked dry gas as shown in Figure 1, tool
Body process please refers to the explanation of above-mentioned separation method, and the technological parameter being related to is as follows：
1) pressure of catalytic cracked dry gas is 1.6MPa.
2) temperature when hydrate working solution enters hydration reactor is 8 DEG C, pressure 5MPa.
3) pressure of the hydrate working solution by the trunnion section of hydration reactor is 1.2MPa.
4) fluid that the hydrogen in hydrate working solution and catalytic cracked dry gas is formed is in the stable section of hydration reactor
Pressure is 4.5MPa.
5) operation temperature of hydrate separator is 9 DEG C, operating pressure 4.3MPa.
6) operation temperature of hydrate neutralizing device is 9 DEG C, operating pressure 0.2MPa.
The composition of the isolated hydrogen-rich gas of technological process through Fig. 1 and hydrogen depleted gas, it is as shown in table 2 below：
The composition of 2 hydrogen-rich gas of table and hydrogen depleted gas
| Composition | CH4 | C2H6 | C2H4 | C3H6 | CO2 | H2 |
| The content of hydrogen-rich gas, mol% | 11.25 | 3.52 | 5.08 | 0.27 | 1.89 | 77.99 |
| The content of hydrogen depleted gas, mol% | 27.38 | 14.93 | 41.59 | 0.10 | 4.48 | 11.50 |
As shown in Table 2, the mole fraction of hydrogen is 77.99% in hydrogen-rich gas, and the rate of recovery of hydrogen has reached 73%, should
The result shows that：Above-mentioned hydration separation method can effectively be detached hydrogen in catalytic cracked dry gas.
Finally it should be noted that：The above embodiments are merely illustrative of the technical solutions of the present invention, rather than its limitations；Although
The present invention is described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that：It still may be used
To modify to the technical solution recorded in foregoing embodiments or carry out equivalent replacement to which part technical characteristic；
And these modification or replace, various embodiments of the present invention technical solution that it does not separate the essence of the corresponding technical solution spirit and
Range.
Claims (6)
1. the separation method of hydrogen in a kind of catalytic cracked dry gas, which is characterized in that including being hydrated catalytic cracked dry gas
Reaction, and the process of hydrogen-rich gas is collected, wherein,
Realize that the hydration reactor of hydration reaction has following structure：Hydration reactor cavity is along hydrate working solution flow direction
With entrance, trunnion section and stable section, and the circulation area of trunnion section is respectively less than the circulation area of entrance and stable section, should
The side wall that hydration reactor cavity corresponds to trunnion section offers air inlet；
The separation method includes：Hydrate working solution is sent into from entrance in the hydration reactor, does catalytic cracking
Gas is connected by air inlet with hydration reactor, and the suction generated using the hydrate working solution for flowing through trunnion section is urged to be separated
Change cracking dry gas sucking hydration reactor, and the two is made to be mixed during stable section is flow to and hydration reaction occurs, generate
Hydrate slurry and hydrogen-rich gas；
The hydrate slurry and hydrogen-rich gas are sent into hydrate separator, detaches and collects hydrogen-rich gas；
Wherein, the internal diameter of the pipeline of the entrance of the hydration reactor is 15-50mm, the internal diameter of the trunnion section and the entrance
For the internal diameter of the pipeline ratio of section for 0.05-0.5, the internal diameter ratio of the diameter of the air inlet and the trunnion section is 0.2-0.5；
The internal diameter of the pipeline ratio of the length of the entrance and the entrance is 1-3, the trunnion segment length and the trunnion
For the internal diameter ratio of section for 1-2.5, the internal diameter of the pipeline ratio of the length of the stable section and the entrance is 3-5.
2. separation method according to claim 1, which is characterized in that make top of the hydrogen-rich gas from hydrate separator
Portion discharges and is collected in outlet, and it is real that outlet at bottom of the hydrate slurry through hydrate separator is sent into hydrate neutralizing device
Neutralizing is applied, dissolves the hydrate working solution of removing gas and is used for hydration reaction cycle.
3. separation method according to claim 1, which is characterized in that when so that the hydrate working solution is entered hydration reactor
Temperature is 4-15 DEG C, pressure 1.0-5.1MPa.
4. separation method according to claim 1, which is characterized in that the operation temperature of the hydrate separator is 4-15
DEG C, operating pressure 1.1-5.1MPa.
5. separation method according to claim 2, which is characterized in that the operation temperature of the hydrate neutralizing device is 8-23
DEG C, operating pressure 0.1-2.1MPa.
6. the separation method according to claim 1 or 3, which is characterized in that catalytic cracked dry gas to be separated is inhaled into hydration
Pressure before reactor is 0.6-1.6MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410495746.4A CN105502289B (en) | 2014-09-24 | 2014-09-24 | The separation method and its system of hydrogen in a kind of catalytic cracked dry gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410495746.4A CN105502289B (en) | 2014-09-24 | 2014-09-24 | The separation method and its system of hydrogen in a kind of catalytic cracked dry gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105502289A CN105502289A (en) | 2016-04-20 |
| CN105502289B true CN105502289B (en) | 2018-06-29 |
Family
ID=55710676
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410495746.4A Expired - Fee Related CN105502289B (en) | 2014-09-24 | 2014-09-24 | The separation method and its system of hydrogen in a kind of catalytic cracked dry gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105502289B (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1301684A (en) * | 1999-12-30 | 2001-07-04 | 中国科学院广州能源研究所 | Method and device for separating and reclaiming ethylene from catalytic cracked dry gas |
| CN103623766A (en) * | 2013-12-10 | 2014-03-12 | 中国科学院广州能源研究所 | Spraying device for rapidly forming gas hydrate |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7128777B2 (en) * | 2004-06-15 | 2006-10-31 | Spencer Dwain F | Methods and systems for selectively separating CO2 from a multicomponent gaseous stream to produce a high pressure CO2 product |
-
2014
- 2014-09-24 CN CN201410495746.4A patent/CN105502289B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1301684A (en) * | 1999-12-30 | 2001-07-04 | 中国科学院广州能源研究所 | Method and device for separating and reclaiming ethylene from catalytic cracked dry gas |
| CN103623766A (en) * | 2013-12-10 | 2014-03-12 | 中国科学院广州能源研究所 | Spraying device for rapidly forming gas hydrate |
Non-Patent Citations (1)
| Title |
|---|
| 水合物法从烟气中分离CO2的原理和实验系统;唐良广 等;《动力工程》;20051031;第25卷;第651页第1栏第3段 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105502289A (en) | 2016-04-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103861444B (en) | A kind of collecting carbonic anhydride based on hydrate and desalinization combined production device and method | |
| CN105498485B (en) | The separation method and its system of methane in a kind of mixed empty coal bed gas | |
| CN103638800B (en) | Utilize the device and method of hydrate continuous batch divided gas flow | |
| CN103585883B (en) | Volatility solvent recovery technology from vent gas and device in a kind of oil plant sulphur unit collection solfatara | |
| CN105502289B (en) | The separation method and its system of hydrogen in a kind of catalytic cracked dry gas | |
| CN103537168B (en) | A kind of technique of pressure in tower when reducing pressure-swing absorber desorb | |
| CN105754673A (en) | Integrated device for natural gas desulphurization and desulfurizing liquid regeneration | |
| CN102464999B (en) | Oil gas absorption recovering method | |
| CN204661332U (en) | A kind of recovery system of potassium catalyzer | |
| CN204746031U (en) | Waste gas washs recovery unit | |
| CN208700784U (en) | Potato starch wastewater defoaming system | |
| CN108569739B (en) | System and method for recovering OP-10 in polytetrafluoroethylene concentrated dispersion liquid waste liquid | |
| CN106380014A (en) | Graded diversion recycling apparatus of hydrogen peroxide production process wastewater | |
| CN206502787U (en) | A kind of removing tar dirt system of coke-stove gas | |
| CN104876188A (en) | Device for recycling hydrogen sulfide generated in production process of viscose filament yarns | |
| CN205055708U (en) | A washing system for methyl alcohol system alkene | |
| CN105498648B (en) | A kind of hydration reactor and the method for mixing methane in empty coal bed gas using reactor separation | |
| CN204385096U (en) | A kind of propylene product protection bed regeneration purge device | |
| CN109200759B (en) | Recovery method of pressure energy of methanol-to-olefin device | |
| CN105477988B (en) | New sulfur reduction process equipment | |
| CN108863702B (en) | Heat recovery system and method for isobutane dehydrogenation process | |
| CN106753632A (en) | A kind of small-sized well head natural gas purification method of purification and device | |
| CN103386286A (en) | Recyclable reaction vessel system | |
| CN207913288U (en) | A kind of cyclohexanol oil-water mixture removes oil recovery system | |
| CN105505464A (en) | A fiber liquid film contactor amine washing desulphurization device and an amine washing desulphurization method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20180629 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |