CN204917998U - Recovery unit of ammonia in coal gasification synthetic gas - Google Patents
Recovery unit of ammonia in coal gasification synthetic gas Download PDFInfo
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- CN204917998U CN204917998U CN201520345349.9U CN201520345349U CN204917998U CN 204917998 U CN204917998 U CN 204917998U CN 201520345349 U CN201520345349 U CN 201520345349U CN 204917998 U CN204917998 U CN 204917998U
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Abstract
The utility model discloses a recovery unit of ammonia in coal gasification synthetic gas, including the cooler, dust remover, scrubber, over heater, water -gas shift catalytic converter, cooling body, the gas -liquid separation mechanism that connect through pipeline order in proper order, washing the ammonia tower, the cooler is connected with the gasifier, washes to be equipped with the synthetic gas in the ammonia tower and to export, and there is the solution heat exchanger in gas -liquid separation mechanism through the tube coupling, and this solution heat exchanger passes through the pipeline to be connected with solution cryrogenic crystallizer, washes ammonia tower adoption demineralized water. The utility model discloses a carrying out hierarchical cooling to the synthetic gas and handling, partial condensation liquid circulates to condensate to last formation carries out sub zero treatment, thereby forms solid particle ammonium bicarbonate, accomplishes the recovery to ammonia in the synthetic gas, but this device wide application in multiple gasification such as air current bed, fluidized bed and fixed bed gasifier.
Description
Technical field
The utility model relates to a kind of ammonia recovery unit, specifically a kind of ammonia in gasification furnace coal preparing synthetic gas recovery and prepare the device of solid ammonium salt.
Background technology
Along with the day of fossil energy especially oil supply is becoming tight, and use the increasingly serious of brought environmental pollution and global warming problem by fossil energy, the mankind are in the urgent need to changing traditional energy expenditure pattern and consumption structure.At present, world energy sources consumption structure has completed the conversion from the solid energy to liquid energy, and starts to transform to Gas Energy Source, and the disposable energy expenditure of China is still based on coal, and proportion is up to about 70%.For realizing the strategical adjustment of China's energy structure, the cleaning coal utilization technology such as gasification obtains broad development in recent years, and the exploitation of new forms of energy simultaneously also receives much concern.Applying of these low stain, low emission technology meets current low-carbon economy Development patterns, is conducive to promoting China's change in the style of economic growth.
In prior art, synthetic gas adopts gasification to prepare substantially.All contain certain gaseous ammonia in the synthetic gas that nearly all gasification is produced, be transformed primarily of nitrogen content of coal, in synthetic gas, particularly gasification condition is relevant, generally between 500 ~ 10000ppmv for ammonia density and gasification process.Synthetic gas is in cooling and washing process, and ammonia is transferred in phlegma or washing water, and because in synthetic gas, concentration is lower, in phlegma and washing water, ammonia content is also lower, between 3 ~ 8%.Adopt in general technology flow process and carry out the mode of steam stripped by ammonia concentrate in phlegma by containing ammoniacal liquor, can liquid pure ammonia be obtained through two steps or multistep.But this process energy consumption is comparatively large, and in the water of concentrate still residual ammonia need process, and the storage of byproduct liquefied ammonia and transhipment require high, its sell be used for agricultural market obviously by the impact in season.
Summary of the invention
The technical problems to be solved in the utility model is to provide the retrieving arrangement of nitrogen in a kind of synthesis gas from coal gasification, by synthesis gas from coal gasification condensate circulation to improve the ammonia density in phlegma, in ammonia at a lower temperature in phlegma and synthetic gas, carbonic acid gas and water react and generate ammonium hydrogencarbonate, ammonium bicarbonate solution is lowered the temperature further, ammonium hydrogencarbonate crystallization, obtains solid carbonic acid hydrogen ammonia byproduct after separation.
In order to solve the problems of the technologies described above, the utility model takes following technical scheme:
The retrieving arrangement of ammonia in a kind of synthesis gas from coal gasification, described retrieving arrangement comprise be linked in sequence successively by pipeline cooler, fly-ash separator, washer, superheater, water-gas shift catalyticreactor, cooling body, gas-liquid separation mechanism, Ammonic washing tower, gas-liquid separation mechanism, cooler is connected with vapourizing furnace, syngas outlet is provided with in Ammonic washing tower, gas-liquid separation mechanism is connected with solution heat exchanger by pipeline, this solution heat exchanger is connected with solution cryogenic crystallization device by pipeline, inputs de-mineralized water in Ammonic washing tower.
Described cooling body comprises the first water cooler, the second water cooler and the 3rd water cooler, and gas-liquid separation mechanism comprises the first gas-liquid separator, the second gas-liquid separator and the 3rd gas-liquid separator; First water cooler, the first gas-liquid separator, the second water cooler, the second gas-liquid separator, the 3rd water cooler and the 3rd gas-liquid separator are linked in sequence successively by pipeline, first cooler inlet end is connected with water-gas shift catalyticreactor, the air outlet end of the 3rd gas-liquid separator is not connected with Ammonic washing tower by pipeline, and the outlet end of the 3rd gas-liquid separator is connected with solution heat exchanger by pipeline.
The outlet end of described first gas-liquid separator is connected with the liquid feeding end of washer by the band pipeline of recycle pump.
The outlet end of the second gas-liquid separator is connected with the outlet of the first water cooler and the import of the 3rd water cooler respectively by the pipeline of band recycle pump.
Described solution heat exchanger is connected by the outlet end of pipeline with the 3rd gas-liquid separator.
The outlet end of described Ammonic washing tower is connected with the liquid feeding end of washer by pipeline.
The utility model by synthesis gas from coal gasification condensate circulation to improve the ammonia density in phlegma, in ammonia at a lower temperature in phlegma and synthetic gas, carbonic acid gas and water react and generate bicarbonate of ammonia, ammonium bicarbonate soln is lowered the temperature further, bicarbonate of ammonia crystallization, solid ammonium bicarbonate byproduct is obtained after separation, effective reduction process energy consumption, reduce the link of production draining simultaneously, play certain good action to environmental protection, solid ammonium bicarbonate byproduct is also easy to store and transport and adjustment in season relatively simultaneously.The utility model device can extensively be suitable for the multiple gasifying process such as air flow bed, fluidized-bed and fixed-bed gasification furnace.
Accompanying drawing explanation
Accompanying drawing 1 is the utility model catenation principle schematic diagram.
Embodiment
For the ease of the understanding of those skilled in the art, below in conjunction with accompanying drawing, the utility model will be further described.
As shown in Figure 1, the utility model discloses the retrieving arrangement of ammonia in a kind of synthesis gas from coal gasification, comprise the cooler 1 be linked in sequence successively by pipeline, fly-ash separator 2, washer 3, superheater 4, water-gas shift catalyticreactor 5, cooling body, gas-liquid separation mechanism, Ammonic washing tower 8, gas-liquid separation mechanism, cooler 1 is connected with vapourizing furnace, this vapourizing furnace exports synthetic gas, syngas outlet is provided with in Ammonic washing tower 8, gas-liquid separation mechanism is connected with solution heat exchanger 9 by pipeline, this solution heat exchanger 9 is connected with solution cryogenic crystallization device 10 by pipeline, de-mineralized water is used in Ammonic washing tower 8.De-mineralized water in Ammonic washing tower washs synthetic gas, and the synthetic gas of discharging from the syngas outlet of Ammonic washing tower is sent to purification system to carry out purifying for use.Wherein washer has water port, to be discharged and to be sent to process by the waste water after washing.Cryogenic crystallization device is that device separated out by ammonium salt, and cryogenic crystallization device contains the outlet of solid ammonium salt and the outlet of lower concentration ammonium salt dilute solution.
Described cooling body comprises the first water cooler 61, second water cooler 62 and the 3rd water cooler 63, and gas-liquid separation mechanism comprises the first gas-liquid separator 71, second gas-liquid separator 72 and the 3rd gas-liquid separator 73; First water cooler 61, first gas-liquid separator 71, second water cooler 62, second gas-liquid separator 72, the 3rd water cooler 63 and the 3rd gas-liquid separator 73 are linked in sequence successively by pipeline, first water cooler 61 entrance end is connected with water-gas shift catalyticreactor 5, the air outlet end of the 3rd gas-liquid separator 63 is not connected with Ammonic washing tower 8 by pipeline, and the outlet end of the 3rd gas-liquid separator 63 is connected with solution heat exchanger 9 by pipeline.Namely the exit end of the first water cooler is connected with the entrance end of the first gas-liquid separator, the outlet side of the first gas-liquid separator is connected with the entrance end of the second water cooler, the exit end of the second water cooler is connected with the entrance end of the second gas-liquid separator, and the outlet side of the second gas-liquid separator is connected with the entrance end of the 3rd water cooler.Wherein, the first water cooler cools to higher synthetic gas, and after cooling, synthetic gas is about 100 DEG C; Second water cooler then cools to from the first water cooler synthetic gas out, and after cooling, synthetic gas is about about 60 DEG C; 3rd water cooler then cools to from the second water cooler synthetic gas out, and after cooling, synthetic gas is about about 40 DEG C.By this classification progressively cooling body, what realize synthetic gas has interim cooling, provides condition for finally generating solid ammonium bicarbonate.Certainly, in case there is a need, level Four or Pyatyi water cooler can also be set, describe in detail no longer one by one at this and enumerate.
In order to carry out recycle to the water of condensation after gas-liquid separation, the outlet end of the first gas-liquid separator is connected with the liquid feeding end of washer by the band pipeline of recycle pump.The outlet end of the second gas-liquid separator is connected with the outlet of the first water cooler and the import of the 3rd water cooler respectively by the pipeline of band recycle pump.And solution heat exchanger is connected by the outlet end of pipeline with the 3rd gas-liquid separator.The outlet end of Ammonic washing tower is connected with the liquid feeding end of washer by pipeline.
Because synthetic gas is discharged afterwards from vapourizing furnace, temperature is higher, and be first down to moderate temperature through cooler from high temperature, then through fly-ash separator, be generally dry collector, after dry gas cleaning, synthetic gas enters in washer and washs.After washing, in synthetic gas, vapour content increases, and after supplementing suitable superheated vapour, then send into and carry out overheated in superheater, the synthetic gas after overheated enters water gas converting catalyst shift-converter, and now the temperature of synthetic gas is about 200 ~ 350 DEG C.Afterwards, synthetic gas just starts to enter classification progressively cooling stages, arranges 3 grades of coolings in the present embodiment altogether.In the 1st grade i.e. the first water cooler, synthetic gas generates a large amount of higher temperatures phlegma through cooling, this phlegma enters laggard row gas-liquid separation in the first gas-liquid separator, the collection and confinement of gases separated is on the first gas-liquid separator top, and the liquid separated is then because own wt sinks to bottom the first gas-liquid separator.Because the condensate temperature separated in the first gas-liquid separator is higher, the ammonia density be dissolved in this phlegma is lower, and therefore this part water directly delivers to washer for synthesis gas washing, realizes the recycling of phlegma.
From the first gas-liquid separator separates synthetic gas out enter into the 2nd grade namely the second water cooler carry out second time and cool, the phlegma of generation moderate temperature, then enter into the second gas-liquid separator and carry out gas-liquid separation.Synthetic gas after separation is collected in the second gas-liquid separator top, and phlegma then sinks to bottom the second gas-liquid separator.The condensate temperature come again due to the second gas-liquid separator separates is medium, higher containing ammonia in its phlegma, therefore, the circulation of the major part of the second gas gas-liquid separator separates phlegma is out delivered to the outlet of the first water cooler, after contacting from the first water cooler synthetic gas out, because the temperature of synthetic gas is higher, phlegma is heated to close to 100 DEG C, ammonia in phlegma also major part is precipitated, and the ammonia be precipitated enters the second water cooler together with synthetic gas.The synthetic gas entering the second water cooler like this containing ammonia density be by from the first cooler outlet containing ammonia synthesis gas add the gaseous ammonia of separating out in the phlegma sent from the second gas-liquid separator and, the ammonia density the synthetic gas of discharging from the second cooler outlet and phlegma is all improved.Except the major part in the phlegma be collected in the second gas-liquid separator being delivered to the outlet of the first water cooler except this, also the small portion of the phlegma in the second gas-liquid separator is injected to the import of the 3rd water cooler, dissolved ammonia in the phlegma that the condensed fluid sprayed into and continuing in the 3rd water cooler generates and carbonic acid gas in synthetic gas and water generate bicarbonate of ammonia, because synthetic gas temperature after the 3rd water cooler cools is lower, the carbonic acid gas under cryogenic in dissolved ammonia and synthetic gas and water are easy to generate bicarbonate of ammonia.And carbonic acid gas is very large relative to the amount of ammonia in synthetic gas, be very beneficial for promoting that ammonia is converted into bicarbonate of ammonia.
Then the solution generated containing ammonium hydrogencarbonate is collected in the 3rd gas-liquid separator.In the synthetic gas of the outlet of the 3rd water cooler, also may contain very small amount of gaseous ammonia, be admitted to Ammonic washing tower with synthetic gas, cleaned in this Ammonic washing tower.Bicarbonate of ammonia containing higher concentration in the phlegma of the 3rd water cooler that the 3rd gas-liquid separator is collected.Under about 40 DEG C conditions, the solubleness of bicarbonate of ammonia is more than 35%, and temperature is just at about 40 DEG C after the cooling of the 3rd water cooler, and the bicarbonate of ammonia therefore generated almost all is dissolved in water.This part phlegma is delivered in solution heat exchanger again and lower the temperature with the clear liquid heat exchange be separated, then enter deep cooling in last solution cryogenic crystallization device.Along with temperature reduces further, the solubleness of the bicarbonate of ammonia in solution declines, part bicarbonate of ammonia crystallization, obtains solid ammonium bicarbonate by also discharging with liquid separation after solid crystal sedimentation; And the clear liquid be separated with precipitated crystal is still containing certain dissolving bicarbonate of ammonia, to be circulated in the second gas-liquid separator separates phlegma out and to be mixed, the ammonia contained in this phlegma then again enters in the 3rd water cooler in circulation thereafter, again generates hydrogen-carbonate crystalline ammonium in the manner described above.Deep freezer generally by low temperature frozen water as coolant cools.
In normal productive process, when the formation speed of the equivalent ammonia in crystallization bicarbonate of ammonia is consistent with the flow of the ammonia come in vapourizing furnace synthetic gas, the ammonia density in each loop of whole device all will be stabilized in certain level.
As with synthetic gas, have small reduction at the ammonia density of the first cooler outlet place synthetic gas than from the ammonia density in the synthetic gas of washing tower, that is because small portion ammonia enters in the higher temperatures phlegma of generation.The ammonia entered after the first gas-liquid separator in the synthetic gas of the second water cooler is improved significantly due to the circulation of the second water cooler phlegma; And because ammonia is more readily dissolved in water under cryogenic in the synthetic gas entering the 3rd water cooler, so in fact gaseous nitrogen content density loss, but then significantly improve containing ammonia in the phlegma accompanied with synthetic gas.
In Ammonic washing tower, the ammonia remained in the 3rd cooler outlet synthetic gas is cooled by de-mineralized water, and lower containing ammonia density in water, this part water send synthesis gas scrubber.
Be described with concrete case study on implementation below.
1, fluidized-bed gasification furnace (air gasification or pure oxygen gasification) syngas outlet temperature is at 800 ~ 1100 DEG C, to 300 ~ 600 DEG C after cooler cooling, through dry gas cleaning, synthetic gas washs in the washers, after washing, synthetic gas temperature is at 135 ~ 190 DEG C, in synthetic gas vapour content increase, through overheated laggard enter catalyzer shift-converter, temperature is at 200 ~ 350 DEG C.Now synthetic gas temperature after the first water cooler reduces to 100 DEG C, be collected in the first gas-liquid separator after a large amount of phlegmas is separated from the gas, synthetic gas enters the second water cooler, after the cooling of the second water cooler, the temperature of synthetic gas is 60 to 80 DEG C, be collected in the second gas-liquid separator after the phlegma generated is separated from the gas, last synthetic gas enters in the 3rd water cooler and again cools, synthetic gas is cooled to 40 DEG C, be collected in the 3rd gas-liquid separator after the phlegma generated is separated from the gas, enter Ammonic washing tower with the synthetic gas of liquid separation and wash away residual ammonia.
2, the pure oxygen gasification of airflow bed gasification furnace or the syngas outlet temperature of air gasification are at 1000 ~ 1300 DEG C, to 300 ~ 600 DEG C after cooling, through dry gas cleaning, synthetic gas washs in washing tower, temperature is at 135 ~ 190 DEG C, in synthetic gas vapour content increase, through overheated laggard enter catalyzer shift-converter, temperature is at 200 ~ 350 DEG C.Now synthetic gas synthetic gas temperature after the first water cooler reduces to 100 DEG C, be collected in the first gas-liquid separator after a large amount of phlegmas is separated from the gas, synthetic gas enters in the second water cooler, temperature out is 60 to 80 DEG C, be collected in the second gas-liquid separator after the phlegma generated is separated from the gas, last synthetic gas enters the 3rd water cooler and synthetic gas is cooled to 40 DEG C, is collected in the 3rd gas-liquid separator after the phlegma of generation is separated from the gas.
3, the pure oxygen gasification of fixed-bed gasification furnace or the syngas outlet temperature of air gasification are at 400 ~ 600 DEG C, gas washing and cooling after to 60 ~ 80 DEG C, through dry gas cleaning, synthetic gas washs in washing tower, temperature is at 135 ~ 190 DEG C, in synthetic gas vapour content increase, through overheated laggard enter catalyzer shift-converter, temperature is at 200 ~ 350 DEG C.Now synthetic gas synthetic gas temperature after the first water cooler reduces to 100 DEG C, be collected in the first gas-liquid separator after a large amount of phlegmas is separated from the gas, synthetic gas enters the second water cooler, temperature out is 60 to 80 DEG C, be collected in the second gas-liquid separator after the phlegma generated is separated from the gas, last synthetic gas enters the 3rd water cooler and synthetic gas is cooled to 40 DEG C, is collected in the 3rd gas-liquid separator after the phlegma of generation is separated from the gas.
It should be noted that, the above is not the restriction to wanting technical solutions of the utility model, and under the prerequisite not departing from creation design of the present utility model, any apparent replacement is all within protection domain of the present utility model.
Claims (6)
1. the retrieving arrangement of ammonia in a synthesis gas from coal gasification, it is characterized in that, described retrieving arrangement comprise be linked in sequence successively by pipeline cooler, fly-ash separator, washer, superheater, water-gas shift catalyticreactor, cooling body, gas-liquid separation mechanism, Ammonic washing tower, cooler is connected with vapourizing furnace, syngas outlet is provided with in Ammonic washing tower, gas-liquid separation mechanism is connected with solution heat exchanger by pipeline, this solution heat exchanger is connected with solution cryogenic crystallization device by pipeline, uses de-mineralized water in Ammonic washing tower.
2. the retrieving arrangement of ammonia in synthesis gas from coal gasification according to claim 1, it is characterized in that, described cooling body comprises the first water cooler, the second water cooler and the 3rd water cooler, and gas-liquid separation mechanism comprises the first gas-liquid separator, the second gas-liquid separator and the 3rd gas-liquid separator;
First water cooler, the first gas-liquid separator, the second water cooler, the second gas-liquid separator, the 3rd water cooler and the 3rd gas-liquid separator are linked in sequence successively by pipeline, first cooler inlet end is connected with water-gas shift catalyticreactor, the air outlet end of the 3rd gas-liquid separator is not connected with Ammonic washing tower by pipeline, and the outlet end of the 3rd gas-liquid separator is connected with solution heat exchanger by pipeline.
3. the retrieving arrangement of ammonia in synthesis gas from coal gasification according to claim 2, is characterized in that, the outlet end of described first gas-liquid separator is connected with the liquid feeding end of washer by the band pipeline of recycle pump.
4. the retrieving arrangement of ammonia in synthesis gas from coal gasification according to claim 3, is characterized in that, the outlet end of the second gas-liquid separator is connected with the outlet of the first water cooler and the import of the 3rd water cooler respectively by the pipeline of band recycle pump.
5. the retrieving arrangement of ammonia in synthesis gas from coal gasification according to claim 4, it is characterized in that, described solution heat exchanger is connected by the outlet end of pipeline with the 3rd gas-liquid separator.
6. the retrieving arrangement of ammonia in synthesis gas from coal gasification according to claim 5, it is characterized in that, the outlet end of described Ammonic washing tower is connected with the liquid feeding end of washer by pipeline.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107118810A (en) * | 2017-05-05 | 2017-09-01 | 北京清创晋华科技有限公司 | It is a kind of to go out the heating of scrubbing tower synthesis gas except the method for aqueous water |
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2015
- 2015-05-26 CN CN201520345349.9U patent/CN204917998U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107118810A (en) * | 2017-05-05 | 2017-09-01 | 北京清创晋华科技有限公司 | It is a kind of to go out the heating of scrubbing tower synthesis gas except the method for aqueous water |
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