CN208732629U - A kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat - Google Patents
A kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat Download PDFInfo
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- CN208732629U CN208732629U CN201821276062.5U CN201821276062U CN208732629U CN 208732629 U CN208732629 U CN 208732629U CN 201821276062 U CN201821276062 U CN 201821276062U CN 208732629 U CN208732629 U CN 208732629U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The utility model relates to a kind of systems for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat, including absorber, generator, condenser Intermediate Heat Exchanger, forecooler and solution force (forcing) pump, the ammonia that generation is heated in the generator enters evaporative condenser by ammonia pipeline, low pressure process gaseous ammonia is sent into absorber by pipeline, poor ammonia solution in the ammonia scrubber becomes rich ammonia solution after absorbing low pressure ammonia, the richness ammonia solution is pumped into exchanger by rich solution force (forcing) pump, enter generator after absorbing heat in exchanger, poor ammonia solution in the generator enters ammonia scrubber after exchanger is cooling.This system is cooled down using the waste heat of soda manufacture process steam condensate liquid to carry out pressure-raising to low-pressure ammonia again, refrigeration or other process applications are carried out to obtain high-pressure liquid ammonia supply Outer Cooler, traditional high-power ammonia refrigerating compressor is substituted, and realizes energy-efficient beneficial effect.
Description
Technical field
The utility model relates to absorption afterheat utilizing systems, and in particular to a kind of to be condensed using soda manufacture process steam
The system that fluid residual heat produces liquefied ammonia.
Background technique
In chemical production process, the reasonable of steam condensed water waste heat utilizes the economic benefit and carbon that are directly related to enterprise
Quantity is discharged, and realizes the only way of sustainable economic development.This part of waste heat is difficult through the prior art again at present
It recycles, while cannot be directly discharged in environment again, can only be handled, be caused in such a way that recirculated cooling water cools down
Great waste.And it needs to consume the low pressure ammonia that outside energy generates technique in connection alkali process and carries out pressure-raising liquid
Change, the gas ammonia of low pressure is compressed to high pressure gas ammonia currently with compressor, consumes additional electric energy.How by steam condensate (SC)
Waste heat be applied to also have become a big project of nowadays Chemical Manufacture business research in connection alkali process.
Utility model content
In order to overcome drawbacks described above, the utility model provides a kind of to be produced using soda manufacture process steam condensation fluid residual heat
The system of liquefied ammonia, the system produce high pressure liquid using the by-product steam condensate (SC) generated in calcination process as drive energy
Ammonia has saved cost so that waste heat is recycled, and reduces energy consumption.
The utility model achieves the above object through the following technical schemes:
A kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat, for using soda manufacture technique
In 150 DEG C of saturated vapor condensed waters of calcination process by-product waste heat driving liquefied ammonia preparation system, including generator, vaporation-type
Condenser, Outer Cooler, ammonia scrubber and exchanger, in which: the generator is equipped with steam condensate import and steam is cold
Condensate outlet is utilized for outputting and inputting 150 DEG C of saturated vapor condensed waters of calcination process by-product in soda manufacture technique
The waste heat of condensed water makes the rich ammonia solution in generator form ammonia, and it is cold that the ammonia output end of the generator is connected to vaporation-type
The input terminal of condenser；The output end of evaporative condenser is connected to the input terminal of Outer Cooler by storage of described liquefied ammonia, by ammonia condensation
It is used at being delivered to after liquefied ammonia in Outer Cooler for other processes；The ammonia output end of Outer Cooler is connected to ammonia scrubber, by liquid
Ammonia is delivered in ammonia scrubber after being converted into low pressure ammonia；The ammonia scrubber is connected by rich solution force (forcing) pump and exchanger
It connects, the rich ammonia solution of formation is transported in exchanger；The input terminal of rich the ammonia solution output end and generator of the exchanger
Connection, the rich ammonia solution in exchanger is transported in generator；The poor ammonia solution output end and exchanger of the generator
The connection of poor ammonia solution input terminal, and the poor ammonia solution output end of exchanger is connect with ammonia scrubber, and being used for will be in generator
Poor ammonia solution be transported in ammonia scrubber after exchanger is cooling.
As the scheme that the utility model advanced optimizes, the generator passes through primary filter and evaporative condenser
Connection, and the primary filter is set to the top of generator.
As the scheme that the utility model advanced optimizes, the primary filter is cold by gas-liquid separator and vaporation-type
Condenser connection.
As the scheme that the utility model advanced optimizes, the fluid output port of the gas-liquid separator is also logical with generator
Piping connection is crossed, for passing through the drop separated in gas-liquid separator in Pipeline transport to generator.
As the scheme that the utility model advanced optimizes, the poor ammonia solution output end of the ammonia scrubber is connected with poor
Liquid circulating pump, the output end of lean solution circulating pump and the top of ammonia scrubber connect, and the lean solution circulating pump is used for poor ammonia is molten
Liquid cyclically sprays in ammonia scrubber.
As the scheme that the utility model advanced optimizes, the exchanger is also connected with cooler, the cooler
Output end is connect with ammonia scrubber.
As the scheme that the utility model advanced optimizes, the cooler is water cooling exchanger, and cooler is equipped with and follows
The inlet and outlet of ring water.
As the scheme that the utility model advanced optimizes, the ammonia scrubber is equipped with fluid level controller, in steam
The pipeline of condensate liquid import connection is equipped with automatic regulating valve, and automatic regulating valve is connect with fluid level controller.
The working process of the utility model is as follows:
150 DEG C of by-product or so of the saturated vapor from calcination process is passed through generation by steam condensate import
Device heats the rich ammonia solution in generator using the waste heat of saturated vapor, makes ammonia and poor ammonia solution,
In, after ammonia removes the liquid being mingled with by gas-liquid separator, it is transported in evaporative condenser, poor ammonia solution is defeated by pipeline
It is sent in exchanger；
Ammonia passes through the saturation liquefied ammonia of the effect generation of evaporative condenser and is stored in storage of described liquefied ammonia, then passes through liquefied ammonia
The pressure of storage tank itself is sent into Outer Cooler for use；
The low pressure ammonia that reaction generates in Outer Cooler is transported in ammonia scrubber, and the poor ammonia solution in ammonia scrubber is inhaled
Become rich ammonia solution after receiving low pressure ammonia；
Rich ammonia solution in ammonia scrubber is transported in exchanger by rich solution force (forcing) pump, and by the richness in exchanger
Ammonia solution is transported in generator；
Poor ammonia solution in generator is transported in exchanger, heat occurs in exchanger for poor ammonia solution and rich ammonia solution
It is transported to after cooler further cools down and is transported in ammonia scrubber after exchange is cooling, and repeat step 3 to make poor ammonia solution
It is recycled.
The utility model has the beneficial effects that:
1) this system using the waste heat of 150 DEG C of saturated vapor condensed waters of calcination process by-product in soda manufacture technique come pair
Low-pressure ammonia carries out pressure-raising and cools down again, to obtain high-pressure liquid ammonia, thus substitutes traditional high-power ammonia refrigerating compressor, thus real
Energy-efficient beneficial effect is showed；
2) 150 DEG C or so of high temperature condensate liquid of the calcination process output of the soda manufacture technique described in, by waste heat benefit
With rear, temperature is down to 100 DEG C hereinafter, therefore avoiding former 150 DEG C of condensate liquids during long distance delivery due to vapor flash
It phenomena such as pipe vibration of generation, noise, excessively high moment pressure, is brought so as to cause rupture and water attack (water hammer) effect of pipe
The safety in production hidden danger such as great destructiveness, the condensate liquid after this cooling first cool down with boiler feedwater heat exchange, then with desalted water
Raw water heat exchange cooling is not needed to be further added by the cooling device with recirculated water, be saved into purification mixed bed as the water supply of boiler
Cost reduces energy consumption；
3) this system is conducive to promoting the use using recycling new technologies of low-grade heat sources such as waste heat and waste heat, reduces
The operation cost of user has good energy-saving and emission-reduction demonstration effect and social benefit in chemical field.
Detailed description of the invention
Fig. 1 is the ammonia pressure-raising liquefaction system schematic diagram of the utility model；
Fig. 2 is the ammonia pressure-raising liquefaction flow path figure of the utility model.
In figure: 10- generator；100- steam condensate entrance；101- steam condensate outlet；11- primary filter；
12- gas-liquid separator；20- evaporative condenser；21- storage of described liquefied ammonia；40- ammonia scrubber；41- lean solution circulating pump；42- rich solution
Force (forcing) pump；50- exchanger；60- cooler；600- water inlet；601- water outlet.
Specific embodiment
The application is described in further detail with reference to the accompanying drawing, it is necessary to it is indicated herein to be, implement in detail below
Mode is served only for that the application is further detailed, and should not be understood as the limitation to the application protection scope, the field
Technical staff can make some nonessential modifications and adaptations to the application according to above-mentioned application content.
A kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat as shown in Figure 1, including occur
Device 10, evaporative condenser 20, ammonia scrubber 40 and exchanger 50, the generator 10 be equipped with steam condensate import and
Steam condensate outlet, the ammonia that generation is heated in the generator 10 enter evaporative condenser 20, ammonia by ammonia pipeline
Gas is condensed into liquefied ammonia and enters storage of described liquefied ammonia 21 by liquefied ammonia pipeline by evaporative condenser 20, in the storage of described liquefied ammonia 21
Liquefied ammonia enters the Outer Cooler 30 in soda ash technique by pipeline, and the low pressure ammonia that reaction generates in Outer Cooler 30 enters ammonia absorption
Device 40, in the ammonia scrubber 40, poor ammonia solution becomes rich ammonia solution after absorbing low pressure ammonia, which passes through rich solution
Force (forcing) pump 42 is pumped into exchanger 50, and generator 10 is entered after absorbing heat in exchanger, and the poor ammonia solution in the generator 10 passes through
Enter ammonia scrubber 40 after exchanger 50 is cooling.
Using the waste heat of 150 DEG C of saturated vapor condensed waters of calcination process by-product of soda manufacture technique to low pressure in this system
Ammonia pressure-raising cools down again, and acquisition high-pressure liquid ammonia is subsequent to be used for soda manufacture technique, thus instead of the ammonia system of one big function rate
Cold compressor realizes energy-efficient effect.By taking calcination process generates 120 tons of 150 DEG C of saturated vapor condensed waters per hour as an example, steam
Vapour condensed water is cooled to 90 DEG C from 150 DEG C and produces 8500Kw heat, and energy a part is used for 0.4MPa low pressure gas ammonia pressure
It is reduced to the high pressure gas ammonia of 1.3MPa, numerical value about 1600Kw；Its excess heat is used to carrying out the solvent of ammonia solution into heating repeatedly to rise
Temperature.Novel polynary refrigeration working medium is used in this system in ammonia solution, will need to press by what helical-lobe compressor was completed originally
Contracting gas is changed into incompressible liquid boosting by pressure-raising process, and electricity is greatly reduced while efficiently using heat sources
It can loss.
Cooler 60 is additionally provided between exchanger 50 and ammonia scrubber 40, the poor ammonia solution come out from exchanger 50
Enter ammonia scrubber 40 after the cooler further cools down.The effect of exchanger 50 is in ammonia scrubber 40
Low temperature richness ammonia solution carries out heat exchange with the poor ammonia solution of high temperature in generator 10, and rich ammonia solution passes through rich solution force (forcing) pump 42
Reaching about 1.3MPa after boosting, generator 10 is entered after the heating of exchanger 50, the pressure of generator is 1.3MPa, therefore from
The poor ammonia solution come out in generator 10 overcomes resistance to reach ammonia scrubber 40 enough.
The cooler 60 is water cooling exchanger, which is equipped with the water inlet 600 and water outlet of recirculated water
601.After poor ammonia solution is further cooled down in cooler 60 by recirculated cooling water, into ammonia scrubber 40, to be conducive to
Absorption of the poor ammonia solution to ammonia.
The ammonia scrubber 40 is also connected with a lean solution circulating pump 41, and the lean solution circulating pump 41 is for recycling poor ammonia solution
Ground is sprayed into ammonia scrubber 40.The lean solution circulating pump 41 effect is to improve sprinkle density, is conducive to suction of the solvent to ammonia
It receives.
Ammonia in the generator 10 successively enters evaporative condenser after primary filter 11 and gas-liquid separator 12
20.The primary filter 11 is to be used to filter out the mist in ammonia except mist device, and gas-liquid separator 12 further will be in ammonia
The drop separation of carrying comes out, the content liquid after above-mentioned twice filter in ammonia be down to 0.1ppmw hereinafter, to
Improve subsequent refrigerating efficiency.Gas-liquid separator uses the product of quite your filter Co., Ltd in the present embodiment.
The primary filter 11 is set to the top of generator 10, and the drop separated in the gas-liquid separator 12 is logical
Pipeline is crossed to return in the generator 10.
The ammonia scrubber 40 is equipped with fluid level controller (not shown), sets in steam condensate inlet ductwork
Automatic regulating valve (not shown) is set, which can condense according to the temperature automatic adjustment steam in generator 10
The uninterrupted of liquid.For the protection to rich solution force (forcing) pump 42, fluid level controller is loaded on ammonia scrubber 40, to guarantee
Force (forcing) pump has enough suction heads, prevents the generation of cavitation and the lubricating fluid of bearing is made to have enough pressure；In rich solution
It is equipped with load-relay (not shown) in the circuit of force (forcing) pump 42, installs temperature on the outlet conduit of rich solution force (forcing) pump 42
Relay (not shown), load-relay is for playing the role of protection to motor and impeller etc.；Temperature relay is used to
Prevent lubricating oil temperature is excessively high from bearing being made to be damaged；In order to guarantee the safety operation of system, it can also be equipped with a spare richness
Liquid force (forcing) pump.
This system economic analysis:
1, the power consumption of this waste heat project calculates
1. the 2 circulating pump power consumptions of UTILIZATION OF VESIDUAL HEAT IN unit, unit internal circulation pump general power is 84kW；
2. needing mating recirculated water 1560m3/ h, recirculated water energy consumption 0.035kWh/m3, circulating water cooling tower fan energy consumption is
1560m3/h×0.035kWh/m3=54.6kW；
3. water circulating pump energy consumption is about twice of blower, i.e. 109.2kW；
The total power consumption of UTILIZATION OF VESIDUAL HEAT IN unit: 84+54.6+109.2=247.8kW；
2, former a set of screw Ammonia Compressor Unit power consumption calculates
1. Ammonia Compressor Unit main motor rated power 1600kW；
2. Oil pump electrical machinery 15Kw in unit, Lubricating-oil Station motor 3Kw, total 18Kw；
3. unit is cooling using evaporative condenser, every set ammonia refrigerating compressor group is equipped with four specified heat exchange amounts and is
The evaporative condenser of 2000kW, every set condenser are equipped with the water pump of a 7.5kW, the blower of two 7.5kW power；
The condenser power consumption of single set unit: 7.5kWx4+7.5kWx8=90kW.
Former a set of total power consumption of ammonia refrigerating compressor: 1600+15+3+90=1708kW.
3, the power cost saved after system operation
Year economic benefit: (1708-247.8) × 8000 × 0.71=8293936 (member)
Wherein, the electricity charge are as follows: 0.71 yuan/degree, calculated by 8000 hours in year；It therefore, 1 year can by using this refrigeration system
To save more than 800 ten thousand power cost.
It is as shown in Figure 2 the working process of the utility model is as follows:
150 DEG C of by-product or so of saturated vapor of the calcination process come enters generator 10 by condensate liquid import, right
Rich ammonia solution in generator is heated, and ammonia and poor ammonia solution are made, and ammonia enters vaporation-type by ammonia pipeline
The poor ammonia solution of condenser 20, high temperature enters exchanger 50；
Ammonia is cooled to saturation liquefied ammonia by evaporative condenser 20, which is flow automatically by liquefied ammonia pipeline stores up into liquefied ammonia
Slot 21 is sent into soda ash process equipment for use using the pressure of storage of described liquefied ammonia itself；
The low pressure ammonia exported in soda ash technique Outer Cooler enters ammonia scrubber 40, the poor ammonia solution in ammonia scrubber
Become rich ammonia solution after absorbing low pressure ammonia；
Rich ammonia solution in ammonia scrubber 40 enters exchanger by rich solution force (forcing) pump.
Poor ammonia solution in generator 10 enters cooler after exchanger 50 is cooling and further cools down, and enters back into ammonia
Absorber 40 repeats the poor ammonia solution of step 3 and is recycled.
150 DEG C or so of high temperature saturated vapor condensate liquid by being heated to rich ammonia solution, itself be reduced to 100 DEG C with
Under, and the low-boiling ammonia of major part in rich ammonia solution is evaporated as high pressure ammonia, rich ammonia solution is because of most ammonia
Gas is evaporated and becomes poor ammonia solution, and poor ammonia solution is by exchanger 50 (carrying out heat exchange with rich ammonia solution) and cooler 60
Enter ammonia scrubber 40 after (using cooling water that poor ammonia solution is cooling) cooling, the poor ammonia solution after being cooled down is more conducive to ammonia
Absorption, after high pressure ammonia passes through evaporative condenser 20, become high-pressure liquid ammonia stand-by, the soda ash technique that enters soda ash process equipment
The low pressure ammonia exported in Outer Cooler enters ammonia scrubber 40 and is absorbed by poor ammonia solution, so as to become rich ammonia molten for poor ammonia solution
Liquid, rich ammonia solution enter generator 10, in the whole process, saturated vapor after exchanger 50 absorbs the heat of poor ammonia solution
The waste heat of condensate liquid is utilized, and is become high-pressure liquid ammonia after low-pressure ammonia air lift pressure and used for subsequent technique.
Above-described embodiments merely represent several embodiments of the utility model, the description thereof is more specific and detailed,
But it should not be understood as limiting the scope of the patent of the utility model.It should be pointed out that for the common of this field
For technical staff, without departing from the concept of the premise utility, various modifications and improvements can be made, these all belong to
In the protection scope of the utility model.
Claims (8)
1. a kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat, for using in soda manufacture technique
150 DEG C of saturated vapor condensed waters of calcination process by-product waste heat driving liquefied ammonia preparation system, which is characterized in that including occur
Device (10), evaporative condenser (20), Outer Cooler (30), ammonia scrubber (40) and exchanger (50), in which: the generator
(10) it is equipped with steam condensate import (100) and steam condensate outlet (101), for by the calcining in soda manufacture technique
150 DEG C of saturated vapor condensed waters of process by-product are output and input, and keep the rich ammonia in generator (10) molten using the waste heat of condensed water
Liquid forms ammonia, and the ammonia output end of the generator (10) is connected to the input terminal of evaporative condenser (20)；Vaporation-type is cold
The output end of condenser (20) is connected to the input terminal of the Outer Cooler (30) in soda ash technique by storage of described liquefied ammonia (21), and ammonia is cold
It is delivered in Outer Cooler (30) after congealing into liquefied ammonia；Outer Cooler (30) output end is connected to ammonia scrubber (40), and liquefied ammonia is converted
At being delivered to after low pressure ammonia in ammonia scrubber (40)；The ammonia scrubber (40) by rich solution force (forcing) pump (42) with exchange
Device (50) connection, the rich ammonia solution of formation is transported in exchanger (50)；The rich ammonia solution output end of the exchanger (50)
It is connect with the input terminal of generator (10), the rich ammonia solution in exchanger (50) is transported in generator (10)；The described hair
The poor ammonia solution output end of raw device (10) is connect with the poor ammonia solution input terminal of exchanger (50), and the poor ammonia of exchanger (50) is molten
Liquid output end is connect with ammonia scrubber (40), is used for the poor ammonia solution in generator (10) after exchanger (50) are cooling
It is transported in ammonia scrubber (40).
2. a kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat according to claim 1,
Be characterized in that, the generator (10) is connect by primary filter (11) with evaporative condenser (20), and it is described at the beginning of imitated
Filter (11) is set to the top of generator (10).
3. a kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat according to claim 2,
It is characterized in that, the primary filter (11) is connect by gas-liquid separator (12) with evaporative condenser (20).
4. a kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat according to claim 3,
It is characterized in that, the fluid output port of the gas-liquid separator (12) is used for also with generator (10) by piping connection by gas-liquid
The drop separated in separator (12) passes through in Pipeline transport to generator (10).
5. a kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat according to claim 1,
It is characterized in that, the poor ammonia solution output end of the ammonia scrubber (40) is connected with lean solution circulating pump (41), lean solution circulating pump
(41) output end is connect with the top of ammonia scrubber (40), and the lean solution circulating pump (41) is used for poor ammonia solution cyclically
It sprays into ammonia scrubber (40).
6. a kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat according to claim 1,
It is characterized in that, the exchanger (50) is also connected with cooler (60), the output end and ammonia scrubber of the cooler (60)
(40) it connects.
7. a kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat according to claim 6,
It is characterized in that, the cooler (60) is water cooling exchanger, and cooler (60) is equipped with water inlet (600) and the water outlet of recirculated water
Mouth (601).
8. a kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat according to claim 1,
It is characterized in that, the ammonia scrubber (40) is equipped with fluid level controller, is equipped on the pipeline of steam condensate import connection
Automatic regulating valve, automatic regulating valve are connect with fluid level controller.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821276062.5U CN208732629U (en) | 2018-08-08 | 2018-08-08 | A kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201821276062.5U CN208732629U (en) | 2018-08-08 | 2018-08-08 | A kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat |
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| CN208732629U true CN208732629U (en) | 2019-04-12 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108726536A (en) * | 2018-08-08 | 2018-11-02 | 安徽沃特普尔节能科技有限公司 | A kind of system and method for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat |
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2018
- 2018-08-08 CN CN201821276062.5U patent/CN208732629U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108726536A (en) * | 2018-08-08 | 2018-11-02 | 安徽沃特普尔节能科技有限公司 | A kind of system and method for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat |
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Address after: 230000 17 Innovation Park, Luyang University, Luyang, Hefei Patentee after: Anhui pupan Energy Technology Co.,Ltd. Address before: 230000 17 Innovation Park, Luyang University, Luyang, Hefei Patentee before: ANHUI WATER POWER ENERGY SAVING TECHNOLOGY Co.,Ltd. |
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