CN201045128Y

CN201045128Y - Axial radial multiple-hearth indirect heat transfer type energy-saving ammonia converter

Info

Publication number: CN201045128Y
Application number: CNU2007200057240U
Authority: CN
Inventors: 伍宏业; 邱文炳; 赵敏
Original assignee: China Huanqiu Engineering Co Ltd
Current assignee: China Huanqiu Engineering Co Ltd
Priority date: 2007-02-16
Filing date: 2007-02-16
Publication date: 2008-04-09
Anticipated expiration: 2017-02-16

Abstract

The utility model discloses an indirect heat transfer style energy-saving ammonia synthetic tower of an axial radial composite bed with three beds and four layers. A layer I of the ammonia synthetic is divided into two layers, namely an upper layer Ia and a lower layer Ib. The upper layer Ia is an axial layer holding a small amount of accelerating agents, the lower Ib is a radial layer, no temperature regulation device is mounted between the upper layer and the lower layer, a bed layer II and a bed layer III are radial fluid beds, a heat transfer is installed between the bed I and the bed II and also between the bed II and the bed III, the upper layer Ia forms air axial flowing, the lower layer Ib forms air radial flowing, the upper layer Ia is filled with a small amount of accelerating agents of middle grain diameters, and the lower layer Ib, the radial fluid bed II and the radial fluid bed III are filled with high active accelerating agents of fine grains. In the manufacturing technique of the synthesis ammonia, the utility model has good energy-saving effect, and a recycle compressor of the utility model consumes only 90% power of the indirect heat transfer style energy-saving ammonia synthetic tower of the axial radial composite bed with multiply beds and layers.

Description

The diameter of axle is to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula

Technical field

The utility model relates to a kind of industrial chemicals production equipment, particularly a kind of ammonia synthesis converter.

Background technology

Ammonia synthesizing industry is the industry of a high energy consumption, and ammonia synthesis converter is the key equipment in the Ammonia Production.

The shortcoming of old-fashioned axial ammonia synthesis converter is the high ammonia net value of operating pressure low (being that combined coefficient is low) and (being compressor power consumption height) falls greatly in reaction gas pressure.For example, be 14.3Mpa from the operating pressure of certain large ammonia converter of external introduction, ammonia net value is～10%, full tower pressure drop is 0.6～1.0Mpa.Because ammonia synthesizing industry is the industry of high energy consumption, reduces cost for enhancing productivity and energy consumption must be lowered.The ton ammonia energy consumption of new with the Sweet natural gas the is energy-saving ammonia synthesis technology of raw material is reduced to present 7,000,000 kilocalories (29.3GJ) from 1,000 ten thousand kilocalories (41.8GJ) of early seventies.Reduce the working pressure (promptly reducing the power consumption of synthetic gas compressed gas) of synthetic tower, adopt high activated catalyst and adopt interchanger to replace the quench gas temperature adjustment, improve the developing direction that temperature (promptly improving the heat utilization efficiency of exhaust gas) that the ammonia net value (promptly raising the efficiency) of ammonia synthesis converter, the inlet and outlet pressure that reduces synthetic tower fall (promptly reducing the recycle compressor power consumption) and improve exhaust gas just becomes modern energy-saving synthetic tower.

Present existing ammonia synthesis converter technology still can not overcome the shortcoming that the ammonia synthesis operating pressure is too high and energy consumption is too high.

Summary of the invention

The utility model is in order to overcome the shortcoming that the ammonia synthesis operating pressure is too high and energy consumption is too high, and provides a kind of three four layers of diameters of axle to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula.

The utility model has adopted following technical scheme: comprise high pressure shell, ammonia converter internals, I bed, II bed, III bed, interchanger, sparger, gas collector, the I bed of described ammonia synthesis converter is divided into two-layer: upper strata Ia is the axial layer that less catalyzer is housed, the Ib of lower floor is a radial layer, does not have temperature control equipment between the upper and lower layer.

Described gas distributor and gas collector are two-layer structure, and wherein one deck is a perforated cylinder, and another layer is whole slotted hole screen net structure.The catalyzer of a small amount of medium grain of filling in the Ia axial flow movable bed of described I bed upper strata.Filling fine particle high activated catalyst in the radial flow bed of the described I bed Ib of lower floor, II bed, III bed.Described interchanger is a shell and tube heat exchanger, and vertically to install along the synthetic tower axle center.The working pressure range that ammonia synthesis converter suits is between 7～30Mpa, and the diameter of reactor is Φ 1600mm～Φ 4000mm.

The utility model compared with prior art, have following beneficial effect: the energy-saving effect in Ammonia Production technology is better, its recycle compressor power consumption only compare with the energy-saving ammonia synthesis converter of multi-bed layer shaft radial multiple-hearth indirect heat exchange formula for its 90%, see energy-conservation comparison sheet:

Energy-conservation comparison sheet

Project	Unit	One two the footpath three	Three four layers	Remarks
Project	Unit	One two the footpath three	Three four layers	Remarks	Throughput		Big-and-middle-sized	Big-and-middle-sized
Operating pressure	Mpa(A)	7～30	7～30		Throughput		Big-and-middle-sized	Big-and-middle-sized
Operating pressure	Mpa(A)	7～30	7～30		The end bed tempertaure	℃	414～445	414～445
Ammonia net value	％	12.4～15.0	12.4～15.8		The end bed tempertaure	℃	414～445	414～445
Ammonia net value	％	12.4～15.0	12.4～15.8		Full tower pressure drop	Mpa	0.25～0.35	0.25～0.30
The recycle compressor power consumption	％	100	90		Full tower pressure drop	Mpa	0.25～0.35	0.25～0.30

Description of drawings

Fig. 1 is the utility model ammonia synthesis converter synoptic diagram

Embodiment

Below in conjunction with accompanying drawing, the utility model specific embodiment is described in further detail.

As shown in Figure 1, three four layers of diameters of axle of the utility model mainly comprise high pressure shell 2, ammonia converter internals 1, I bed, II bed, III bed, interchanger i, sparger and gas collector to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula.The I bed of described ammonia synthesis converter is divided into two-layer, and upper strata Ia is the axial layer that less catalyzer is housed, and the Ib of lower floor is a radial layer, does not have temperature control equipment between the upper and lower layer.Described II and III bed are radial flow bed, are being provided with interchanger between the I-II bed and between the II-III bed.The catalyzer of a spot of medium particle diameter of described I bed upper strata Ia filling, Ib of lower floor and II, III bed filling fine particle high activated catalyst.The catalyzer of a spot of medium particle diameter of described I bed upper strata Ia filling, Ib of lower floor and II, III bed filling fine particle high activated catalyst.Gas distributor and the gas collector of described Ib, II, III are bilayer structure: one deck is a perforated cylinder, and one deck is whole slotted hole silk screen.Described ammonia synthesis converter working pressure range is between 7～30MPa, and the diameter of reactor is Φ 1600mm～Φ 4000mm.

Whole ammonia converter internals 1 is put into synthetic tower high pressure shell 2, synthetic raw gas inlet A at the bottom of the tower enters, enter annular space 3 between internals 1 and the High Pressure Shell 2 by internals 1 bottom skirt perforate, inlet tower gas arrives tower top through annular space 3 and enters interchanger ii tube side downwards from pipe core 4, in order to cool off the reacted gas of II bed (flowing at shell side), its gas is heated itself;

The tube side that upwards enters interchanger i through the unstripped gas after once heating again is in order to cool off the reacted gas of I bed (flowing at shell side), simultaneously itself is entered I bed upper strata Ia to the reaction of I bed catalyst after temperature required by second-heating, Ia bed gas axially flows downward on I bed upper strata, goes out I bed upper strata Ia and enters the I bed Ib of lower floor and carry out adiabatic reaction as radial flow.After reactant gases after temperature raises goes out that the I bed Ib of lower floor bed enters annular space 5, the shell side that enters interchanger I again is cooled to II bed temperature in by the tube side inlet tower gas, enter annular space 6, gas enters the II bed equably from the gas distributor of annular space 6 by the II bed, the gas radial flow is crossed catalyst bed in the II bed, continue to do adiabatic reaction and generate ammonia, then, reaction gas enters II bed gas collector, flows out equably to enter annular space 7.

Reaction gas enters interchanger ii shell side after by annular space 7, entered annular space 8 after the cooling of the inlet tower gas of interchanger II tube side, gas distributor by the III bed enters the III bed equably and makes radial flow and the further synthetic ammonia that generates of adiabatic reaction, temperature raise the back from III bed gas collector flow out equably enter annular space 9 after, flow into escape pipe 10, at high temperature go out tower through outlet B.

Mouth of pipe C is for regulating the by-pass interface of I bed catalyst temperature of reaction, and mouth of pipe D is for regulating the by-pass interface of II bed catalyst temperature of reaction; Variable valve on the inlet line of gas inlet A can be regulated the temperature of reaction of III bed.

Claims

1. a diameter of axle is to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula, comprise high pressure shell, ammonia converter internals, I bed, II bed, III bed, interchanger, sparger, gas collector, the I bed that it is characterized in that described ammonia synthesis converter is divided into two-layer: upper strata Ia is the axial layer that catalyzer is housed, the Ib of lower floor is a radial layer, does not have temperature control equipment between the upper and lower layer.

2. the diameter of axle according to claim 1 is to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula, and its spy is that described II and III bed are radial flow bed, is being provided with interchanger between the I-II bed and between the II-III bed.

3. the diameter of axle according to claim 1 is to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula, and its spy is the gas axial flow among the I bed upper strata Ia, and the Ib gas in the lower floor is made radial flow.

According to claim 1 or the 3 described diameters of axle to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula, it is characterized in that the catalyzer of the medium particle diameter of I bed upper strata Ia filling; Ib of lower floor and II, III bed filling fine particle high activated catalyst.

5. the diameter of axle according to claim 1 is to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula, and it is characterized in that gas distributor and the gas collector of described Ib, II, III is bilayer structure: one deck is a perforated cylinder, and one deck is whole slotted hole silk screen.

6. the diameter of axle according to claim 1 is characterized in that to the energy-saving ammonia synthesis converter of multiple-hearth indirect heat exchange formula: described ammonia synthesis converter working pressure range is between 7～30MPa; The diameter of reactor is Φ 1600mm～Φ 4000mm.