CN206660641U - The converting means that stripping process is applied in coal water slurry gasification - Google Patents
The converting means that stripping process is applied in coal water slurry gasification Download PDFInfo
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- CN206660641U CN206660641U CN201720276510.0U CN201720276510U CN206660641U CN 206660641 U CN206660641 U CN 206660641U CN 201720276510 U CN201720276510 U CN 201720276510U CN 206660641 U CN206660641 U CN 206660641U
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- stripper
- pipeline
- tower bottom
- steam
- liquid
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 22
- 230000008569 process Effects 0.000 title claims abstract description 20
- 238000002309 gasification Methods 0.000 title claims abstract description 18
- 239000003245 coal Substances 0.000 title claims abstract description 15
- 239000002002 slurry Substances 0.000 title claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 79
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 45
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 22
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000010025 steaming Methods 0.000 claims 1
- 230000003851 biochemical process Effects 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 230000008901 benefit Effects 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 8
- 230000009466 transformation Effects 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- DDJSLGMHWKYCDI-UHFFFAOYSA-N azane carbon monoxide Chemical group N.[C-]#[O+] DDJSLGMHWKYCDI-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000003250 coal slurry Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000010797 grey water Substances 0.000 description 1
- 239000013529 heat transfer fluid Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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Abstract
The converting means that stripping process is applied in the coal water slurry gasification that the utility model is related to, including stripper, condensate liquid preheater and gas-liquid separator tank, also include tower bottom reboiler, with being connected in the middle part of stripper at the top of the tower bottom reboiler, the bottom of tower bottom reboiler goes reboiler pipeline to be connected with stripper bottom by condensate liquid, and the upper and lower part of tower bottom reboiler goes tower bottom reboiler pipeline and condensate liquid return pipe webmaster line to be connected with steam respectively；Pass through the technical program, steam is no longer directly filled into stripper, reduce stripper load, so that the condensing liquid quantity of stripper bottom is reduced, therefore the condensing liquid quantity for delivering to buck process is decreased, so as to effectively reduce buck and biochemical process load, the setting of tower bottom reboiler causes the steam that heating uses not contacted directly with liquid containing ammonia condensing, the operating cost of equipment is greatly reduced, reaches water saving, the purpose of energy-conservation, so as to create more preferably economic benefit.
Description
Technical field
A kind of coal water slurry gasification Ammonia Production equipment is the utility model is related to, more particularly in a kind of coal water slurry gasification
The converting means of stripping process application.
Background technology
In coal water slurry gasification production of synthetic ammonia, water-coal-slurry acts on obtaining qualified process gas through gasification furnace and change furnace
While, feed coal can convert ammonification with the nitrogen reaction in oxygen, the constantly accumulation and two in process gas in systems of these ammonia
Carbonoxide forms NH4HCO3Crystallization, pipeline, valve are blocked, so as to influence the normal operation of production equipment.
In order to remove the ammonia in process gas, Ammonic washing tower is set after change furnace, using desalted water and process gas counter current contacting,
Ammonia stripping in gas is got off, liquid containing ammonia condensing caused by Ammonic washing tower bottom is delivered into transformation system stripper, through steam stripping
The condensate liquid that ammonia content declines is obtained afterwards and delivers to the utilization of gasification ash water system circulation, and the stripping tower top exhaust steam containing high strength ammonia is then sent
Burnt to flare system.
Using directly steam is filled into stripper middle part, upflowing vapor contains the stripper of current domestic transformation system with tower top
Ammonia condensing liquid counter current contacting is stripped, and the steam filled into produces new condensate liquid and entered because of heating liquid containing ammonia condensing and itself temperature drop
In stripping tower bottom condensate liquid, meanwhile, flare system is sent into stripping tower top exhaust steam containing high strength ammonia, caused cold after torch burning
Lime set is recycled to transformation system stripper again；So circulation so that system condensing liquid treating capacity is continuously increased, and receives condensation
The gasification ash water of liquid and the increase of biochemical process load, while also increase overhaul of the equipments frequency and expense.
Utility model content
In view of this, main purpose of the present utility model is in the change that stripping process is applied in a kind of coal water slurry gasification is provided
Changing device, by the technical program, the defects of overcoming coal water slurry gasification transformation system stripping process existing process, longtime running
Can condensate liquid treating capacity in reduction system, so as to effectively reduce stripper steam consumption, process gasification ash water after reduction
And biochemical load, the classified utilization of condensate liquid is realized, so as to effectively compensate for the deficiencies in the prior art.
In order to achieve the above object, the technical solution of the utility model is realized in：Vapour in a kind of coal water slurry gasification
The converting means of technique application, including stripper, condensate liquid preheater and gas-liquid separator tank are carried, is set in the middle part of the stripper
There is steam to enter stripper pipeline, stripper top is provided with stripping tower top exhaust steam pipeline, and stripper bottom is provided with condensate liquid and gone
Grey water pipeline, condensate liquid preheater one end are connected with system liquid containing ammonia condensing feed-line, the condensate liquid preheater other end and vapour
Stripper top is connected, and the other end of stripping tower top exhaust steam pipeline is connected with condensate liquid preheater top, condensate liquid preheater bottom
With being connected in the middle part of gas-liquid separator tank, gas-liquid separator tank top goes flare line to be connected with stripping exhaust steam, gas-liquid separator tank
Bottom is connected with stripper top, in addition to tower bottom reboiler, is connected at the top of the tower bottom reboiler with the middle part of stripper
Logical, the bottom of tower bottom reboiler goes reboiler pipeline to be connected with stripper bottom by condensate liquid, the top of tower bottom reboiler
Tower bottom reboiler pipeline and condensate liquid return pipe webmaster line is gone to be connected with steam respectively with bottom.
As further technical scheme, the entrance location that the steam in the middle part of the stripper enters stripper pipeline is higher than tower
Entrance location at the top of the reboiler of bottom with being connected in the middle part of stripper.
As further technical scheme, the steam goes on tower bottom reboiler pipeline to be provided with regulating valve.
It is using the beneficial effect after above-mentioned technical proposal：The converting means that stripping process is applied in coal water slurry gasification, lead to
The technical program is crossed, no longer directly fills into steam to stripping tower bottom, reduces stripper load so that the condensation of stripper bottom
Liquid measure is reduced, therefore decreases the condensing liquid quantity for delivering to buck process, is born so as to effectively reduce buck and biochemical process
Lotus, the setting of reboiler cause the steam that heating uses not contacted directly with liquid containing ammonia condensing, and steam caused by reboiler condenses
Liquid can be recycled to desalted water pipe network and recycle, and the classification processing for realizing condensate liquid utilizes, and greatly reduces the fortune of equipment
Row cost, reach water saving, the purpose of energy-conservation, so as to create more preferably economic benefit.
Brief description of the drawings
Fig. 1 is the utility model transformation system stripping process schematic flow sheet.
In figure, 1 stripper, 2 tower bottom reboilers, 3 condensate liquid preheaters, 4 gas-liquid separator tanks, 5 system liquid containing ammonia condensing
Feed-line, 6 condensate liquid dedusting water pipelines, 7 condensate liquids go reboiler pipeline, 8 stripping tower top exhaust steam pipelines, 9 stripping exhaust steam to go
Flare line, 10 steam enter stripper pipeline, 11 steam remove tower bottom reboiler pipeline, 12 condensate liquid return pipe webmaster lines, 13 regulation
Valve.
Embodiment
The technical solution of the utility model is described in further detail with specific embodiment below in conjunction with the accompanying drawings.
The converting means that stripping process is applied in the coal water slurry gasification that the utility model is related to, including stripper 1, condensate liquid
Preheater 3 and gas-liquid separator tank 4, the middle part of stripper 1 are provided with steam and enter stripper pipeline 10, and the top of stripper 1 is set
Be equipped with stripping tower top exhaust steam pipeline 8, the bottom of stripper 1 is provided with condensate liquid dedusting water pipeline 6, the one end of condensate liquid preheater 3 with
System liquid containing ammonia condensing feed-line 5 is connected, and the other end of condensate liquid preheater 3 is connected with the top of stripper 1, strips tower top exhaust steam
The other end of pipeline 8 is connected with the top of condensate liquid preheater 3, the bottom of condensate liquid preheater 3 and the middle part phase of gas-liquid separator tank 4
Even, the top of gas-liquid separator tank 4 goes flare line 9 to be connected with stripping exhaust steam, the bottom of gas-liquid separator tank 4 and the top of stripper 1
It is connected, in addition to tower bottom reboiler 2, the top of tower bottom reboiler 2 are connected with the middle part of stripper 1, tower bottom reboiler 2
Bottom go reboiler pipeline 7 to be connected with the bottom of stripper 1 by condensate liquid, the upper and lower part of tower bottom reboiler 2 difference
Tower bottom reboiler pipeline 11 and condensate liquid return pipe webmaster line 12 is gone to be connected with steam.
The entrance location that steam as the middle part of stripper described in further embodiment 1 enters stripper pipeline 10 is higher than tower
The entrance location that the top of bottom reboiler 2 is connected with the middle part of stripper 1.
As further embodiment, the steam goes on tower bottom reboiler pipeline 11 to be provided with regulating valve 13.
The utility model at work, stripping tower bottom 1 draw by the steam stripped condensate liquid relatively low containing ammonia to bottom of towe again
Device 2 is boiled, vaporization is heated by steam, the biphase gas and liquid flow being vaporized is sent back to stripper 1 and used as stripped vapor；
The top of stripper 1 obtains what the exhaust steam containing high strength ammonia sent system ammonia condensing liquid feed-line 5 through subcooling condensate preheater 3
Liquid containing ammonia condensing preheats, and enters knockout drum 4 after itself cooling, after separation, flare line 9 is removed by vapour by stripping exhaust steam
Carry gas and deliver to flare system, the condensate liquid after a small amount of separation is recycled to stripper 1 and stripped again；Into tower bottom reboiler 2
Steam is recycled to condensate liquid return pipe webmaster line 12 and recycled with forming condensate liquid after bottom of towe condensed heat transfer fluid；Enter bottom of towe to boil again
The quantity of steam of device 2 removes the tune of tower bottom reboiler pipeline 11 by steam according to the head temperature of stripper 1 and bottom of towe condensate liquid composition
Section valve 13 is adjusted；Remain original steam and enter stripper pipeline 10, when ammonia in the bottom of towe condensate liquid of stripper 1 content compared with
Gao Shi, stripper pipeline 10 can be suitably entered by steam and carries out supplementing steam to reduce the composition of the tower bottom ammonia of stripper 1.
In actual production, using a set of conversion gas as 155000Nm3Exemplified by/h converting means, implemented by the technical program
Afterwards, the 5T/h steam that former stripper 1 directly fills into exits completely, procedure calls after the bottom of towe condensate liquid ammonia content of stripper 1 meets,
Caused steam condensate is all recycled to condensate liquid return pipe net by condensate liquid return pipe webmaster line 12.
Tower bottom reboiler 2 is added in the technical solution of the utility model, avoids steam from being directly added into stripper 1, is accumulated
System condensing liquid treating capacity, steam produce steam by the indirectly heat of tower bottom reboiler 2 so that steam condensate realizes classification profit
With.
It is described above, preferably possible embodiments only of the present utility model, it is not limited to of the present utility model
Scope.
Claims (3)
1. the converting means that stripping process is applied in a kind of coal water slurry gasification, including stripper, condensate liquid preheater and gas-liquid point
From device tank, steam being provided with the middle part of the stripper and enters stripper pipeline, stripper top is provided with stripping tower top exhaust steam pipeline,
Stripper bottom is provided with condensate liquid dedusting water pipeline, condensate liquid preheater one end and system liquid containing ammonia condensing feed-line phase
Even, the condensate liquid preheater other end is connected with stripper top, strips the other end and condensate liquid preheater of tower top exhaust steam pipeline
Top is connected, and with being connected in the middle part of gas-liquid separator tank, gas-liquid separator tank top is gone with stripping exhaust steam for condensate liquid preheater bottom
Flare line is connected, and gas-liquid separator pot bottom is connected with stripper top, it is characterised in that including tower bottom reboiler, institute
State at the top of tower bottom reboiler with being connected in the middle part of stripper, the bottom of tower bottom reboiler by condensate liquid go reboiler pipeline and
Stripper bottom is connected, and tower bottom reboiler pipeline and condensate liquid return pipe are removed in the upper and lower part of tower bottom reboiler with steam respectively
Webmaster line is connected.
2. the converting means that stripping process is applied in coal water slurry gasification according to claim 1, it is characterised in that the vapour
The entrance location that steam in the middle part of stripper enters stripper pipeline is entered higher than at the top of tower bottom reboiler with what is be connected in the middle part of stripper
Mouth position.
3. the converting means that stripping process is applied in coal water slurry gasification according to claim 1, it is characterised in that the steaming
Vapour goes on tower bottom reboiler pipeline to be provided with regulating valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720276510.0U CN206660641U (en) | 2017-03-21 | 2017-03-21 | The converting means that stripping process is applied in coal water slurry gasification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720276510.0U CN206660641U (en) | 2017-03-21 | 2017-03-21 | The converting means that stripping process is applied in coal water slurry gasification |
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| Publication Number | Publication Date |
|---|---|
| CN206660641U true CN206660641U (en) | 2017-11-24 |
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| CN201720276510.0U Active CN206660641U (en) | 2017-03-21 | 2017-03-21 | The converting means that stripping process is applied in coal water slurry gasification |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109734104A (en) * | 2018-11-27 | 2019-05-10 | 重庆建峰化工股份有限公司 | A kind of device and method of the periodic off-gases system production ammonium hydroxide using synthesis ammonia |
| CN112479289A (en) * | 2020-12-09 | 2021-03-12 | 恒力石化（大连）炼化有限公司 | Ammonia nitrogen treatment device for water slurry gasification ash water |
-
2017
- 2017-03-21 CN CN201720276510.0U patent/CN206660641U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109734104A (en) * | 2018-11-27 | 2019-05-10 | 重庆建峰化工股份有限公司 | A kind of device and method of the periodic off-gases system production ammonium hydroxide using synthesis ammonia |
| CN109734104B (en) * | 2018-11-27 | 2022-02-08 | 重庆建峰化工股份有限公司 | Device and method for producing ammonia water by using purge gas system of synthetic ammonia |
| CN112479289A (en) * | 2020-12-09 | 2021-03-12 | 恒力石化（大连）炼化有限公司 | Ammonia nitrogen treatment device for water slurry gasification ash water |
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