CN112742047A - Method and device for pumping negative pressure of urea production evaporation system - Google Patents
Method and device for pumping negative pressure of urea production evaporation system Download PDFInfo
- Publication number
- CN112742047A CN112742047A CN202011633427.7A CN202011633427A CN112742047A CN 112742047 A CN112742047 A CN 112742047A CN 202011633427 A CN202011633427 A CN 202011633427A CN 112742047 A CN112742047 A CN 112742047A
- Authority
- CN
- China
- Prior art keywords
- hydraulic ejector
- stage
- section
- evaporation
- ejector
- 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.)
- Pending
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
- C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
- C07C273/14—Separation; Purification; Stabilisation; Use of additives
- C07C273/16—Separation; Purification
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of urea production, and particularly relates to a method and a device for pumping negative pressure of an evaporation system in urea production. The invention adds water into the circulation tank to a set liquid level, starts the circulation pump to cool the liquid in the circulation tank through the cooler, and then respectively conveys the liquid into the first section hydraulic ejector and the second section hydraulic ejector to provide power sources for the first section hydraulic ejector and the second section hydraulic ejector. The invention uses the hydraulic ejector which can be recycled to pump negative pressure to the urea production evaporation system, and uses the power medium of the hydraulic ejector as water, and recycles the water produced by the urea production evaporation system to the hydraulic ejector, thereby avoiding the waste of steam condensate water resource caused by the traditional ejector adopting low-pressure steam as power, greatly reducing the production cost of enterprises and the environmental protection pressure, and simultaneously, the invention can not cause harm to the environment, and is beneficial to the environment-friendly construction.
Description
Technical Field
The invention belongs to the field of urea production, and particularly relates to a method and a device for pumping negative pressure of an evaporation system in urea production.
Background
In a urea production plant, the discharge of the urea synthesis column is made from NH3、CO2、NH4COONH2、CO(NH2)2、H2The quinary system gas-liquid mixture composed of O, most of unreacted materials after separation and recovery in the unreacted material decomposition and recovery system are called urine, and the quinary system gas-liquid mixture comprises the following components: ur 68% (wt), H2O:29％(wt)、NH3:1.5％(wt)、CO20.5% (wt) into the urine bath. The urine in the urine tank is pressurized by a urine pump and sent into an evaporation system to complete the separation of water in the urine, and the urine is concentrated to 99.7 percent (wt) and sent into a granulator for granulation. The urine is separated from water in evaporation system by negative pressure heating, and the water is separated in the form of water vapor and condensed into NH3Collecting 4-6 wt% ammonia water in an ammonia water tank. And the ammonia water is treated into qualified wastewater containing ammonia of not more than 5PPm in a subsequent desorption system and is discharged.
The negative pressure forming method of the prior urine in an evaporation system is that NH is contained in the urine from an evaporation separator3The water vapor firstly enters a primary surface condenser to lead most of the water vapor to contain NH3The water vapor is condensed into ammonia water and collected into an ammonia water tank by means of potential difference. A small amount of non-condensed NH-containing gas in the primary surface cooler3The water vapor is pumped by a steam jet pump to enter a secondary surface cooler, condensed into ammonia water in the secondary surface cooler and collected into an ammonia water tank by means of potential difference. The evaporation system forms negative pressure in the evaporation separator by means of the suction action of the steam jet pump, and the negative pressure value in the evaporation separator is controlled by controlling the steam pressure entering the steam jet.
The negative pressure pumping of the traditional evaporation system of the urea device is brought by a steam ejector, and power steam and water vapor containing NH3 from an evaporation separator are mixed together and enter an evaporation surface cooler to be condensed into ammonia water to enter an ammonia water tank. Because the ejector power steam and the NH 3-containing steam from the evaporation separator are mixed together, steam condensate generated by the ejector power steam cannot be recycled independently, and the condensate generated by the ejector power steam also enters the ammonia water tank to form ammonia water. The ejector power steam condensate enters the ammonia water tank, so that the water inflow of the ammonia water tank is increased, and the ammonia water load and the environmental protection pressure of the device for processing the subsequent desorption hydrolysis system are increased.
Although ammonia water is treated by a subsequent analytic hydrolysis system to obtain NH3Qualified desorption waste liquid with the content of less than 5PPm is discharged into a trench as qualified waste water for treatment, but the qualified waste water is discharged more and is accumulative pollution to the environment, and meanwhile, ejector power steam condensate cannot be usedRecycling is also a waste for enterprises, and increases the production cost and environmental protection pressure of enterprises.
Disclosure of Invention
In order to overcome the above-mentioned drawbacks of the prior art, the present invention provides a method and a device for extracting negative pressure in an evaporation system for urea production. The invention has the advantages of reducing the production cost of enterprises and reducing the environmental protection pressure of the enterprises.
In order to achieve one of the purposes, the invention adopts the following technical scheme:
a method for pumping negative pressure of an evaporation system in urea production comprises the following steps:
s1: and adding water into the circulation tank to a set liquid level, starting a circulation pump to cool the liquid in the circulation tank through a cooler to form circulating pressure water, and respectively conveying the circulating pressure water into the first-stage hydraulic ejector and the second-stage hydraulic ejector to serve as power sources.
S2: the first-stage hydraulic ejector and the second-stage hydraulic ejector respectively pump the uncondensed gas in the first-stage evaporation surface cooler and the second-stage evaporation surface cooler by utilizing the energy of pressure reduction and throttling of the circulating pressure water, so that the pressure in the first-stage evaporation separator and the second-stage evaporation separator is pumped to a negative pressure state.
S3: and liquid in the first-section hydraulic ejector and liquid in the second-section evaporation ejector both flow back to the circulation tank and are used for providing power sources for the first-section hydraulic ejector and the second-section hydraulic ejector by the circulation pump.
Preferably, the uncondensed gas of the first-stage evaporation surface cooler is sent to a gas inlet of the first-stage hydraulic ejector through an uncondensed gas outlet pipe; and the uncondensed gas of the second-stage evaporation surface cooler is sent to a gas inlet of a second-stage hydraulic ejector through a second-stage uncondensed gas outlet pipe.
Preferably, the level value of the circulation tank in step S1 is 80%.
Preferably, the water vapor containing NH3 in the first-stage evaporation surface cooler comes from a first-stage evaporation separator, and the pressure in the first-stage evaporation surface cooler is controlled within the range of 45KPa to 55KPa by controlling the water pressure entering a first-stage hydraulic ejector through a first-stage liquid inlet valve in the step S1.
Preferably, the water vapor containing NH3 in the secondary evaporation surface cooler comes from a secondary evaporation separator, and the pressure in the secondary evaporation surface cooler is controlled within the range of 8KPa to 15KPa by controlling the water pressure entering the secondary hydraulic ejector through a secondary liquid inlet valve in the step S1.
Preferably, in step S1, the liquid in the first stage hydraulic ejector and the liquid in the second stage evaporation ejector both flow into the circulation tank by means of a head difference.
Preferably, when the concentration of the uncondensed gas dissolved in the circulating pressure water of the first-stage hydraulic ejector and the second-stage hydraulic ejector reaches a set value, a small amount of fresh desalted water is fed into the circulating tank, a small amount of circulating liquid is discharged to the ammonia water tank, and the liquid level and the concentration in the circulating tank are kept stable.
In order to realize the second purpose of the invention, the device for pumping the negative pressure of the urea production evaporation system comprises a circulation tank, a first-section hydraulic ejector, a second-section hydraulic ejector, a first-section evaporation surface cooler and a second-section evaporation surface cooler, wherein the circulation tank is respectively connected with the first-section hydraulic ejector and the second-section hydraulic ejector through a cooler, a gas inlet of the first-section hydraulic ejector is connected with the first-section evaporation surface cooler, and a gas inlet of the second-section hydraulic ejector is connected with the second-section evaporation surface cooler.
Preferably, the circulation tank is connected to the cooler by a circulation pump.
Preferably, the cooler is connected with the first-section hydraulic ejector 1 through a first-section liquid inlet valve, and the cooler is connected with the second-section hydraulic ejector through a second-section liquid inlet valve.
The invention has the advantages that:
(1) the invention uses the water power which can be recycled to suck the non-condensable gas in the urea production device to evaporate the gas out of the gas surface cooler through the water power ejector to pump the negative pressure of the evaporation system. The waste of steam condensate water resources caused by using steam as the motive steam of the ejector is avoided, and the production cost and the environmental protection pressure of enterprises are greatly reduced. The invention does not cause harm to the environment and is beneficial to environment-friendly construction.
(2) The hydraulic ejector of the invention utilizes the liquid level difference to flow the liquid inside into the circulating tank, and does not need to use power, thereby reducing the production cost and saving resources.
Drawings
FIG. 1 is a schematic flow chart of the present invention.
The notations in the figures have the following meanings:
1-circulation tank, 2-cooler, 31-first-stage hydraulic ejector, 32-second-stage hydraulic ejector, 41-first-stage evaporation surface cooler, 42-second-stage evaporation surface cooler, 51-first-stage evaporation separator, 52-second-stage evaporation separator and 6-circulation pump.
Detailed Description
As shown in fig. 1, a method for pumping negative pressure of an evaporation system in urea production comprises the following steps:
s1: adding water into the circulation tank 1 to a set liquid level, starting the circulation pump 6 to cool the liquid in the circulation tank 1 through the cooler 2, and then respectively conveying the liquid into the first-stage hydraulic ejector 31 and the second-stage hydraulic ejector 32 to provide power sources for the first-stage hydraulic ejector 31 and the second-stage hydraulic ejector 32.
S2: the first-stage hydraulic ejector 31 and the second-stage hydraulic ejector 32 respectively pump uncondensed gas (uncondensed NH in the surface cooler) in the first-stage evaporation surface cooler 41 and the second-stage evaporation surface cooler 42 by using the energy of the pressure-reduced throttling of the circulating pressure water3Water vapor) so that the pressure in the first-stage vaporization separator 51 and the second-stage vaporization separator 52 is drawn to a negative pressure state.
S3: the liquid in the first-stage hydraulic ejector 31 and the liquid in the second-stage evaporation ejector both flow back into the circulation tank 1, and the circulation pump 6 is used for providing power sources for the first-stage hydraulic ejector 31 and the second-stage hydraulic ejector 32.
The uncondensed gas of the first-stage evaporation surface cooler 41 is sent to a gas inlet of the first-stage hydraulic ejector 31 through an uncondensed gas outlet pipe; the uncondensed gas of the second-stage evaporation surface cooler 42 is sent to a gas inlet of the second-stage hydraulic ejector 32 through a second-stage uncondensed gas outlet pipe. The level value of the circulation tank 1 in step S1 was 80%. In the step S1, the water pressure entering the first section of the hydraulic ejector is controlled through the first section of the liquid inlet valve, and the technological index of the pressure is 45KPa-55 KPa. In step S1, the water pressure entering the secondary hydraulic ejector 32 is controlled by a secondary liquid inlet valve, and the process index of the pressure is 8KPa-15 KPa. In step S1, the liquid in the first stage hydraulic ejector 31 and the liquid in the second stage evaporation ejector both flow into the circulation tank 1 by means of a head difference. When the concentration of the uncondensed gas dissolved in the circulating pressure water of the first-stage hydraulic ejector 31 and the second-stage hydraulic ejector 32 reaches a set value, the liquid in the circulating water tank is discharged.
A device for pumping negative pressure of an evaporation system in urea production comprises a circulation tank 1, a first-section hydraulic ejector 31, a second-section hydraulic ejector 32, a first-section evaporation surface cooler 41 and a second-section evaporation surface cooler 42, wherein the circulation tank 1 is respectively connected with the first-section hydraulic ejector 31 and the second-section hydraulic ejector 32 through a cooler 2, a gas inlet of the first-section hydraulic ejector 31 is connected with the first-section evaporation surface cooler 41, and a gas inlet of the second-section hydraulic ejector 32 is connected with the second-section evaporation surface cooler 42.
The circulation tank 1 is connected to the cooler 2 by a circulation pump 6. The cooler 2 is connected with the first-section hydraulic ejector 31 through a first-section liquid inlet valve, and the cooler 2 is connected with the second-section hydraulic ejector 32 through a second-section liquid inlet valve.
The following is an example of a device producing 30 million tons of urea per year, and the technical effect obtained by comparing the invention with the comparative example (i.e. by using a swallow-type injector before improvement) is shown in the following table:
1. as shown in the following table 1, the device for producing 30 ten thousand tons of urea annually has an evaporation system for pumping negative pressure and related data before and after technical modification.
TABLE 1
2. Accounting for economic benefits
2.1, the evaporation system is vacuumized, and the steam saving value of a hydraulic ejector is calculated:
comparative example: the evaporation system adopts a steam ejector to vacuumize, and consumes 6 tons of low-pressure steam per hour.
The invention comprises the following steps: the evaporation system adopts a hydraulic ejector to vacuumize and does not consume low-pressure steam. Compared with the method adopting a steam ejector to vacuumize, the method can save low-pressure steam by 6t/h per hour, the low-pressure steam per ton is calculated according to 80 yuan, and the annual effective production time is calculated according to 300 days.
The annual evaporation system adopts the hydraulic ejector to vacuumize, and adopts the steam ejector to vacuumize relatively, saves the low-pressure steam value annually:
6t/h × 24h/d × 300d/y × 80 yuan/t-345.6 ten thousand yuan/year
2.2 the evaporation system adopts a hydraulic ejector to vacuumize, so that the amount of generated ammonia is reduced, and the value of low-pressure steam consumed during the subsequent analysis and hydrolysis system treatment is reduced:
comparative example: the evaporation system adopts a steam ejector to generate ammonia water, and the ammonia water needs to consume 1.5t/h of low-pressure steam in the subsequent treatment of the desorption system.
The invention comprises the following steps: the evaporation system adopts a hydraulic ejector, low-pressure steam is not consumed, the generation amount of ammonia water is not increased, and therefore the low-pressure steam is saved by 1.5t/h in a subsequent analysis system.
The low-pressure steam of each ton is calculated according to 80 yuan, the annual effective production time is calculated according to 300 days, the annual evaporation system adopts a hydraulic ejector to vacuumize, the amount of generated ammonia is reduced, and the value of the low-pressure steam consumed when the amount of generated ammonia is treated by a subsequent analytic hydrolysis system is reduced:
1.5t/h × 24h/d × 300d/y × 80 yuan/t 86.4 ten thousand yuan/year
2.3 circulating Pump Power consumption value calculation
The circulating pump consumes 30Kw/h of electric energy when normally operating, and the price of electricity is calculated according to 1 yuan Kw/h, and the annual effective production time is calculated according to 300 days, and the circulating pump consumes the electric energy value when normally operating throughout the year:
30Kw/h x 24h/d x 300d/y x 1 yuan/Kw.h 21.6 ten thousand yuan/year
2.4 the evaporation system adopts hydraulic jet to pump negative pressure, thereby saving value each year
The negative pressure pumping of the evaporation system every year adopts a hydraulic ejector to save the value of low-pressure steam of 345.6 ten thousand yuan + the hydrolysis system is analyzed every year to reduce the amount of ammonia water to save the value of low-pressure steam of 86.4 ten thousand yuan and the value of electric quantity consumed by a circulating pump of 21.6 ten thousand yuan to 410.4 ten thousand yuan
3. Environmental protection benefit
The evaporation system adopts a hydraulic ejector to pump negative pressure, and a steam ejector to pump negative pressure, so that the production amount of ammonia water can be reduced by 6 tons per hour, and the produced 6 tons of ammonia water consumes 1.5 tons of low-pressure steam to be directly added into the ammonia water when the subsequent desorption hydrolysis system is used for processing, therefore, the negative pressure pumping of the evaporation system adopts the hydraulic ejector to reduce the discharge amount of desorption waste liquid (1.5+6) per hour to 7.5 tons;
the effective production time of the whole year is calculated according to 300 days, and the evaporation system adopts a hydraulic ejector to pump negative pressure to reduce NH content3About 5PPm of desorption effluent discharge.
7.5t/h×24h/d×300d/y＝54000m3/y
The operation of the device is described in detail below with reference to the drawings in the examples.
Adding water into the first floor circulation tank 1 until the water level reaches 80%, opening an inlet valve of the circulation pump 6, starting the circulation pump 6, opening an outlet valve of the circulation pump 6, cooling the liquid in the circulation tank 1 through the cooler 2, and then respectively conveying the liquid to a first-stage hydraulic ejector 31 and a second-stage hydraulic ejector 32 positioned on the fourth floor of the urea device. The first-stage hydraulic ejector 31 and the second-stage hydraulic ejector 32 use the energy of the decompression throttling of the circulating pressure water to suck the uncondensed gas in the surface cooler, and the pressure in the first-stage evaporation separator 51 and the second-stage evaporation separator 52 is pumped to a negative pressure state. Controlling the water pressure entering the first section of hydraulic ejector 31 through a liquid inlet valve, and controlling the pressure in the first section of evaporation separation 41 to be within a process index of 45KPa-55 KPa; the water inlet pressure of the second-stage hydraulic ejector 32 is controlled through a liquid inlet valve, and the pressure in the second-stage evaporation separation 42 is controlled to be 8KPa-15 KPa. The liquid from the first section of hydraulic ejector 31 enters the circulation tank 1 through a liquid outlet pipe, and the liquid from the second section of hydraulic ejector 32 enters the circulation tank 1 through the liquid outlet pipe.
The invention is not to be considered as limited to the specific embodiments shown and described, but is to be understood to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
Claims (10)
1. A method for pumping negative pressure of an evaporation system in urea production is characterized by comprising the following steps:
s1: adding water into the circulation tank (1) to a set liquid level, starting the circulation pump (6) to cool the liquid in the circulation tank (1) through the cooler (2) to form circulating pressure water, and respectively conveying the circulating pressure water into the first-stage hydraulic ejector (31) and the second-stage hydraulic ejector (32) to serve as power sources.
S2: the first-stage hydraulic ejector (31) and the second-stage hydraulic ejector (32) respectively pump the uncondensed gas in the first-stage evaporation surface cooler (41) and the second-stage evaporation surface cooler (42) by utilizing the energy of pressure reduction throttling of the circulating pressure water, so that the pressure in the first-stage evaporation separator (51) and the second-stage evaporation separator (52) is pumped to a negative pressure state.
S3: and liquid in the first-stage hydraulic ejector (31) and liquid in the second-stage evaporation ejector both flow back to the circulation tank (1) and are used for providing power sources for the first-stage hydraulic ejector (31) and the second-stage hydraulic ejector (32) by the circulation pump (6).
2. The method for extracting negative pressure from an evaporation system for urea production as claimed in claim 1, wherein: the uncondensed gas of the first section of evaporation surface cooler (41) is sent to a gas inlet of a first section of hydraulic ejector (31) through a first section of uncondensed gas outlet pipe; the non-condensed gas of the second-stage evaporation surface cooler (42) is sent to a gas inlet of a second-stage hydraulic ejector (32) through a second-stage non-condensed gas outlet pipe.
3. The method for extracting negative pressure from an evaporation system for urea production as claimed in claim 1, wherein: the level value of the circulation tank (1) in the step S1 is 80%.
4. The method for extracting negative pressure from an evaporation system for urea production as claimed in claim 1, wherein: the vapor containing NH3 in the first-stage evaporation surface cooler (41) comes from a first-stage evaporation separator (51), the water pressure entering a first-stage hydraulic ejector is controlled through a first-stage liquid inlet valve in the step S1, and the pressure in the first-stage evaporation surface cooler (41) is controlled within the range of 45KPa to 55 KPa.
5. The method for extracting negative pressure from an evaporation system for urea production as claimed in claim 1, wherein: the vapor containing NH3 in the secondary evaporation surface cooler (42) comes from a secondary evaporation separator (52), the water pressure entering a secondary hydraulic ejector (32) is controlled by a secondary liquid inlet valve in the step S1, and the internal pressure of the secondary evaporation surface cooler (52) is controlled within the range of 8KPa-15 KPa.
6. The method for extracting negative pressure from an evaporation system for urea production as claimed in claim 1, wherein: in the step S1, the liquid in the first-stage hydraulic ejector (31) and the liquid in the second-stage evaporation ejector both flow into the circulation tank (1) by means of a head difference.
7. The method for extracting negative pressure from an evaporation system for urea production as claimed in claim 1, wherein: when the concentration of the non-condensed gas dissolved in the circulating pressure water of the first-stage hydraulic ejector (31) and the second-stage hydraulic ejector (32) reaches a set value, a small amount of fresh desalted water is supplemented into the circulating tank (1), a small amount of circulating liquid is discharged to the ammonia water tank, and the liquid level and the concentration in the circulating tank (1) are kept stable.
8. A device for extracting negative pressure in an evaporation system for urea production according to claims 1-7, characterized in that: the device comprises a circulation tank (1), a first-section hydraulic ejector (31), a second-section hydraulic ejector (32), a first-section evaporation surface cooler (41) and a second-section evaporation surface cooler (42), wherein the circulation tank (1) is respectively connected with the first-section hydraulic ejector (31) and the second-section hydraulic ejector (32) through a cooler (2), a gas inlet of the first-section hydraulic ejector (31) is connected with the first-section evaporation surface cooler (41), and a gas inlet of the second-section hydraulic ejector (32) is connected with the second-section evaporation surface cooler (42).
9. The apparatus of claim 8, wherein the negative pressure pumping unit comprises: the circulating tank (1) is connected with the cooler (2) through a circulating pump (6).
10. The apparatus of claim 8, wherein the negative pressure pumping unit comprises: the cooler (2) is connected with the first-section hydraulic ejector (31) through the first-section liquid inlet valve, and the cooler (2) is connected with the second-section hydraulic ejector (32) through the second-section liquid inlet valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011633427.7A CN112742047A (en) | 2020-12-31 | 2020-12-31 | Method and device for pumping negative pressure of urea production evaporation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011633427.7A CN112742047A (en) | 2020-12-31 | 2020-12-31 | Method and device for pumping negative pressure of urea production evaporation system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112742047A true CN112742047A (en) | 2021-05-04 |
Family
ID=75650950
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011633427.7A Pending CN112742047A (en) | 2020-12-31 | 2020-12-31 | Method and device for pumping negative pressure of urea production evaporation system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112742047A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113578086A (en) * | 2021-08-18 | 2021-11-02 | 山东联盟化工股份有限公司 | Production process of urea solution for vehicles |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2585995Y (en) * | 2002-12-17 | 2003-11-12 | 金持中 | Aerated water jetting vacuum extractor for tech of urea prodn. |
| CN102389639A (en) * | 2011-11-07 | 2012-03-28 | 毕节金河化工有限公司 | Urea solution evaporation and concentration equipment |
| CN203183709U (en) * | 2013-03-18 | 2013-09-11 | 浙江华康药业股份有限公司 | Evaporative concentration equipment |
-
2020
- 2020-12-31 CN CN202011633427.7A patent/CN112742047A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2585995Y (en) * | 2002-12-17 | 2003-11-12 | 金持中 | Aerated water jetting vacuum extractor for tech of urea prodn. |
| CN102389639A (en) * | 2011-11-07 | 2012-03-28 | 毕节金河化工有限公司 | Urea solution evaporation and concentration equipment |
| CN203183709U (en) * | 2013-03-18 | 2013-09-11 | 浙江华康药业股份有限公司 | Evaporative concentration equipment |
Non-Patent Citations (1)
| Title |
|---|
| 万德波等: "水喷射器在尿素蒸发系统的应用", 《氮肥技术》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113578086A (en) * | 2021-08-18 | 2021-11-02 | 山东联盟化工股份有限公司 | Production process of urea solution for vehicles |
| CN113578086B (en) * | 2021-08-18 | 2023-10-27 | 山东联盟化工股份有限公司 | Production process of urea solution for vehicles |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102190341B (en) | Stripping ammonia-removing method based on flash evaporation and heat pump technologies | |
| CN111302899B (en) | Ammonia and tertiary butanol recovery device and method in cyclohexanone ammoximation production process | |
| CN103145287A (en) | Method for recovering ammonia and synthesis gas from coking wastewater | |
| CN112742047A (en) | Method and device for pumping negative pressure of urea production evaporation system | |
| CN104843816A (en) | Method for combined production of ammonium sulfate and ammonia water through heat pump flash evaporation, stripping and deamination | |
| CN103933831B (en) | A kind of recovery method producing ammonia in 4-5 amido benzotrifluoride technique | |
| CN104003564A (en) | Wet-process rare earth smelting high ammonia-nitrogen wastewater resource utilization method and device | |
| CN103408467A (en) | Low-energy-consumption urea production technology and system adopting CO2 stripping method | |
| CN212222702U (en) | High-efficient low temperature negative pressure ammonia nitrogen waste water strip system | |
| CN216662543U (en) | High pressure fine coal gasification black water low pressure flash distillation device | |
| CN108467049B (en) | System for retrieve ammonia in follow tombarthite separation waste liquid | |
| CN104058475A (en) | Novel heat pump distillation deamination energy-saving process | |
| CN204151096U (en) | A kind of industry contains pre-treatment and the heat reclamation device of ammonia sewage | |
| CN109231331B (en) | CO removal of sludge digestion biogas slurry2Special deamination device and process | |
| CN102583865A (en) | Pretreatment method for waste water in production of phenolic resin | |
| CN210215568U (en) | Recovery system of chlorine gas generated in copper electrolysis extraction process | |
| CN212102637U (en) | Ammonia and tert-butyl alcohol recovery device in cyclohexanone ammoximation production process | |
| CN214936748U (en) | Ammonia distillation system | |
| CN211367028U (en) | Low boiling point grease class contains salt waste water multiple-effect evaporation processing system | |
| CN108178470B (en) | Method for one-step recovery of phosphorus from algae mud by supercritical water gasification | |
| CN113842753A (en) | Treatment process of tail gas discharged from cathode of nitrogen trifluoride electrolytic cell | |
| CN220449809U (en) | System for heat pump flash distillation strip deamination produces ammonium sulfate and aqueous ammonia | |
| CN203355325U (en) | Ethyl alcohol material pressure reduction distillation equipment | |
| CN220736235U (en) | Evaporation system with wet vacuum suction device for urea production | |
| CN220078877U (en) | High concentration ammonia nitrogen evaporation condensation water film processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210504 |